PROCESS FOR RECOVERY OF PROPYLENE AND LPG FROM FCC FUEL GAS USING STRIPPED MAIN COLUMN OVERHEAD DISTILLATE AS ABSORBER OIL

A process is disclosed for enhanced recovery of propylene and LPG from the fuel gas produced in Fluid catalytic cracking unit by contacting a heavier hydrocarbon feed with FCC catalyst. In the conventional process, the product mixture from FCC main column overhead comprising naphtha, LPG and fuel gas, are first condensed and gravity separated to produce unstabilized naphtha, which is subsequently used in the absorber to absorb propylene and LPG from fuel gas. However, the recovery of propylene beyond 97 wt % is difficult in this process since unstabilized naphtha already contains propylene of 5 mol % or above. In the present invention, Cand lighter components from unstabilized naphtha are first stripped off in a separate column to obtain a liquid fraction almost free from propylene (<0.1 mol %) and other LPG components. Such a stripped liquid fraction, after cooling to 20° C. to 30° C., is used in the absorber to absorb higher amounts of propylene and LPG from fuel gas, leading to improved recovery of propylene. 2. The process as claimed in claim 1 , wherein the main fractionator overhead condenser pressure is from about 10 psig and above claim 1 , preferably 25 psig and above.3. The process as claimed in wherein the stripped naphtha is supplied to the absorber at lower temperatures preferably between from about 20° C. to about 30° C. using chilled water as an indirect cooling media wherein recovery of propylene and other C-Ccomponents is further improved.4. The process as claimed in claim 1 , wherein the debut bottom recycle and absorber oil from external inter-stage coolers is supplied to absorber at about 20° C. to 30° C. by using chilled water as cooling media in cooling exchangers.5. A process as claimed in claim 1 , wherein the gaseous fraction from the absorber optionally further treated before leaving the FCC gas concentration section as Fuel gas.6. (canceled) The invention relates to a process for the enhanced recovery of propylene and LPG from the fuel gas ...

Solvent Extraction Process for Removal of Naphthenic Acids and Calcium from Low Asphaltic Crude Oil

The present disclosure provides a process for obtaining extracted crude oil (ECO) which is substantially free of naphthenic acids, calcium and other impurities from low asphaltic crude oils or their residue fractions by preferential extraction of saturates using at least one solvent. 1. A process for obtaining extracted crude oil (ECO) which is substantially free of naphthenic acids , calcium and other impurities from low asphaltic crude oils or their residue fractions; said process comprising the following steps:a) subjecting the low asphaltic crude oil to preferential extraction of saturates using at least one solvent by vigorously mixing the asphaltic crude oil in at least one form selected from the group consisting of low asphaltic crude oil as such, atmospheric residue of low asphaltic crude oil and vacuum residue of low asphaltic crude oil to obtain a mixture;b) heating the mixture and allowing the heated mixture to settle under gravity to obtain a biphasic mixture with a top layer containing extracted crude oil and solvent and a bottom layer with raffinate containing naphthenic acid, calcium and other impurities;c) separating the top layer from the biphasic mixture; andd) heating the separated top layer to separate the solvent from the extracted crude oil to obtain solvent free extracted crude oil(ECO), said solvent free extracted crude oil being characterized by TAN percentage reduction ranging between 25 to 100%, calcium percentage reduction ranging between 40 to 99%, nickel percentage reduction ranging between 75 to 95%, vanadium percentage reduction ranging between 65 to 95%, sulphur percentage reduction between 2 to 45%, nitrogen percentage reduction ranging between 25 to 50% and CCR percentage reduction ranging between 75 to 97%; said percentages reductions being calculated on the basis of the respective proportions of these impurities in the asphaltic crude oil which is the starting material as employed in method step a.2. The process as claimed in ...

PROCESS FOR OBTAINING VANADIUM OXIDE FROM A GASIFIER SLAG FIELD

A process for obtaining vanadium component in the form of vanadium oxide from gasifier slag is disclosed. The process comprises pulverizing the slag to obtain pulverized slag, which is blended with water and an alkali salt to obtain a slurry. The slurry is dried and then roasted in the presence of air to obtain a roasted slag. The roasted slag is leached to obtain a first filtrate comprising the vanadium component. The first filtrate is reacted with a magnesium salt to remove a silica component in the form of a precipitate. The silica free second filtrate is reacted with an ammonium salt to obtain ammonium metavanadate, which is further calcined to obtain the significant amount of vanadium pentoxide (VO). 1. A process for obtaining vanadium oxide from gasifier slag having vanadium component;the process comprising the following steps:a) pulverizing the gasifier slag to a particle size less than 100 μm to obtain a pulverized slag;b) blending the pulverized slag with water and at least one alkali salt to obtain a slurry;c) drying the slurry to remove water therefrom;d) roasting the dried slurry in the presence of air and at a temperature in the range of 750° C. to 1000° C. to obtain a roasted slag;e) leaching the roasted slag with water to obtain a first filtrate comprising the vanadium component;f) separating a silica component from the first filtrate to obtain a second filtrate;g) reacting the second filtrate with an ammonium salt to obtain ammonium metavanadate in the form of a precipitate; andh) separating the precipitate and calcining at a temperature in the range of 400 to 600° C. to obtain vanadium oxide having purity greater than 95%.2. The process as claimed in claim 1 , wherein in the step (b) the alkali salt is at least one selected from the group consisting of sodium carbonate (NaCO) and sodium sulphate (NaSO) and the amount of the alkali salt is in the range of 20 wt % to 50 wt % of the total slag.3. The process as claimed in claim 1 , wherein in the step ...

PROCESS AND COMPOSITION OF CATALYST/ADDITIVE FOR REDUCING FUEL GAS YIELD IN FLUID CATALYTIC CRACKING (FCC) PROCESS

The present invention relates to a catalyst for Fluid Catalytic Cracking (FCC) which contains a combination of a FCC catalyst component and an additive component with certain physical properties attributed therein. The present invention is also directed to provide methods for the preparation of the catalyst for FCC. The admixture of the FCC catalyst component and additive component is used in cracking of hydrocarbon feedstock containing hydrocarbons of higher molecular weight and higher boiling point and/or olefin gasoline naphtha feedstock for producing lower yield of fuel gas with out affecting the conversion and yield of general cracking products such as gasoline, propylene and Colefins. 1. A process for cracking of higher boiling petroleum feedstock to obtain lower dry gas without affecting the yield of LPG , light olefins and gasoline products; said process comprising the steps of:contacting said feedstock under reaction conditions suitable for fluid catalytic cracking with a catalyst comprising:(a) a FCC catalyst component comprising:at least one zeolite in an amount ranging between 5 and 95 wt %;at least one clay in an amount ranging between 5 and 40 wt %;at least one binder in an amount ranging between 5 and 40 wt %;at least one alkaline earth metal in an amount ranging between 0.01 and 2.0 wt %; andat least one rare earth metal in an amount ranging between 0.01 and 2.0 wt %; and(b) an additive component comprising:at least one zeolite in an amount ranging between 5 and 95 wt %;at least one clay in an amount ranging between 5 and 40 wt %;at least one binder in an amount ranging between 5 and 40 wt %;at least one alkaline earth metal in an amount ranging between 0.01 and 2.0 wt %; andat least one phosphorous containing compound in an amount ranging between 0.2 and 55 wt %,all proportion being with respect to the weight of the respective components.2. The process as claimed in claim 1 , wherein the catalyst is adapted to reduce lower dry gas production in the ...

AN FCC CATALYST ADDITIVE AND A PROCESS FOR PREPARATION THEREOF

The present disclosure relates to an FCC catalyst additive for cracking of petroleum feedstock and a process for its preparation. The FCC catalyst additive of the present disclosure comprises at least one zeolite, at least one clay, at least one binder, phosphorous in the form of PO, and at least one Group IVB metal compound. The FCC catalyst additive of the present disclosure is hydrothermally stable and has improved matrix surface area even after various hydrothermal treatments. The FCC catalyst additive of the present disclosure can be used in combination with the conventional FCC catalyst for catalytic cracking to selectively enhance the propylene and LPG yields. 1. An FCC catalyst additive comprisingi. at least one zeolite in an amount in the range of 30 to 50 wt %;ii. at least one clay in an amount in the range of 5 to 40 wt %;iii. at least one binder in an amount in the range of 5 to 20 wt %;{'sub': 2', '5, 'iv. POin an amount in the range of 5 to 10 wt %; and'}v. at least one Group IVB metal compound in an amount in the range of 0.1 to 10 wt %.2. The FCC catalyst additive as claimed in claim 1 , wherein said zeolite is at least one selected from the group consisting of ZSM-5 claim 1 , ZSM-11 claim 1 , and ZSM-22 zeolite.3. The FCC catalyst additive as claimed in claim 1 , wherein said zeolite is ZSM-5 in an amount in the range of 40 to 50 wt %.4. The FCC catalyst additive as claimed in claim 1 , wherein said clay is at least one selected from the group consisting of kaolin clay claim 1 , halloysite claim 1 , bentonite and mixtures thereof.5. The FCC catalyst additive as claimed in claim 1 , wherein said binder is at least one selected from the group consisting of colloidal silica claim 1 , colloidal alumina claim 1 , pseduoboehmite alumina claim 1 , bayrite alumina claim 1 , gamma alumina and mixtures thereof.6. The FCC catalyst additive as claimed in claim 1 , whereinsaid clay is kaolin clay in an amount in the range of 10 to 20 wt %; andsaid binder is ...

STABILIZED INORGANIC OXIDE SUPPORTS AND ADSORBENTS DERIVED THEREFROM FOR CARBON DIOXIDE CAPTURE

The present invention relates to a stabilized inorganic oxide support for capturing carbon dioxide from gases having high regeneration capacities over many cycles. The method for preparing the stabilized inorganic oxide support includes stabilizing an alumina-containing precursor by either calcining or steaming, impregnating an alkali or alkaline earth compound into the stabilized alumina-and drying the alkali or alkaline earth compound-impregnated stabilized alumina-. The stabilized inorganic oxide support can be regenerated at lower temperatures between 100 and 150° C. The carbon dioxide adsorption capacity of the regenerated support is between 70 and 90% of the theoretical carbon dioxide adsorption capacity. 1. A method for preparing a stabilized inorganic oxide support for capturing carbon dioxide from gases , said method comprising the following steps:a. stabilizing at least one alumina-containing precursor selected from the group consisting of gamma-alumina, silica-alumina, boehmite, pseudoboehmite and gibbsite by thermally treating said alumina-containing precursor to obtain a stabilized alumina, wherein the thermal treatment is carried out using at least one technique selected from the group consisting of calcination and steaming;b. impregnating at least one alkali or alkaline earth compound into the stabilized alumina to obtain an alkali or alkaline earth compound-impregnated stabilized alumina, wherein the alkali or alkaline earth compound is at least one compound selected from the group consisting of alkali or alkaline earth carbonates, alkali or alkaline earth bicarbonates and alkali or alkaline earth oxides; andc. drying the alkali or alkaline earth compound-impregnated stabilized alumina, wherein the step of drying is carried out at a temperature in the range of 80° C. to 140° C., preferably at 120° C., to obtain a stabilized inorganic oxide support.2. The method of claim 1 , wherein said stabilized alumina contains at least one alumina form selected ...

System and Method for Preparing Hydrocarbon Blend from Multiple Component Streams

A computer implemented blend control system and method for preparation of a hydrocarbon blend from a plurality of components drawn from respective component tanks have been disclosed. The system, in accordance with the present disclosure includes at least one sensing and analyzing means adapted to sense and analyze a first attribute of at least one of the components for obtaining first attribute data. The system further includes, at least one optimizing means having a data storage means for storing attribute based model data. The optimizing means receives the first attribute data and transmits the received first attribute data to a comparator means which computes an optimized proportion data between each of the component streams to enable selective drawing of each of the component streams in accordance with the optimized proportion data for preparing the hydrocarbon blend. 1. A computer implemented blend control system for preparation of a hydrocarbon blend from a plurality of components drawn from respective component tanks , said system comprising:a) at least one sensing and analyzing means adapted to sense and analyze a first attribute of at least one of the components for obtaining first attribute data; and i) a data storage means for storing attribute based model data;', 'ii) a receiving means for receiving the first attribute data; and', 'iii) a comparator means adapted to compare the first attribute data with the attribute based model data, the comparator means further adapted to compute an optimized proportion data between each of the component streams to enable selective drawing of each of the component streams in accordance with the optimized proportion data for preparing the hydrocarbon blend., 'b) at least one optimizing means having2. The blend control system as claimed in further comprising a flow regulating means operatively connected to the at least one optimizing means and individual component tanks claim 1 , said flow regulating means adapted to ...

Computer Implemented Blend Control System and Method for Preparation of a Hydrocarbon Blend

A computer implemented blend control system and method for preparation of a hydrocarbon blend from a plurality of component streams have been disclosed. The system includes a product tank for receiving a mixture comprising the plurality of component streams. The system further includes a sensing and analyzing means adapted to sense and analyze a first attribute of the received mixture for obtaining a first attribute data. The system further includes an optimizing means which stores the attribute based model data, receives the first attribute data and compares the received first attribute data with the attribute based model data to compute an optimized proportion data, based on which the component streams are selectively drawn into the product tank for preparing the hydrocarbon blend. 1. A computer implemented blend control system for preparation of a hydrocarbon blend from a plurality of component streams , said system comprising:a) a product tank for receiving a mixture comprising the plurality of component streams;b) at least one sensing and analyzing means adapted to sense and analyze a first attribute of the received mixture for obtaining a first attribute data; and i) data storage means for storing attribute based model data,', 'ii) receiving means for receiving said first attribute data, and', 'iii) comparator means adapted to compare the first attribute data with the model data, the comparator means further adapted to compute an optimized proportion data between each of streams in the plurality of component streams to enable selective drawing of the component streams into the product tank for preparing the hydrocarbon blend., 'c) at least one optimizing means having,'}2. The blend control system as claimed in claim 1 , further comprising a flow regulating means cooperating with the at least one optimizing means and to the product tank claim 1 , the flow regulating means adapted to control the flow of the component streams into the product tank based on the ...

Process for Reducing Oxygenate Content of Hydrocarbon Feed

The present disclosure provides a process for reducing oxygenate content of hydrocarbon feed. The process comprises passing and heating the hydrocarbon feed over ion exchange resin resident in a reactor, maintained at a temperature in the range of 90 to 140° C. and a predetermined pressure, at a predetermined liquid hourly space velocity to obtain a heated intermediate fluid. The heated intermediate fluid is cooled to obtain a cooled intermediate fluid. The cooled intermediate fluid is mixed with water to obtain a mixture. The mixture is allowed to settle to obtain an aqueous phase and an organic phase. The aqueous phase is separated from the organic phase to obtain hydrocarbon feed with reduced oxygenate content. The process is simple and environment friendly, enabling removal of 70-90% of the oxygenate content from the hydrocarbon feed. 1. A process for reducing oxygenate content of hydrocarbon feed , said process comprising the following steps:(i) passing and heating said hydrocarbon feed over ion exchange resin resident in a reactor, maintained at a temperature in the range of 90 to 140° C. and at a pre-determined pressure, at a predetermined liquid hourly space velocity to obtain a heated intermediate fluid;(ii) cooling said heated intermediate fluid to obtain a cooled intermediate fluid;(iii) mixing said cooled intermediate fluid with water to obtain a mixture;(iv) allowing said mixture to settle to obtain an aqueous phase and an organic phase; and(iv) separating said aqueous phase from said organic phase to obtain hydrocarbon feed with reduced oxygenate content.2. The process as claimed in claim 1 , wherein said oxygenate in said hydrocarbon feed comprises at least one of methyl tertiary butyl ether (MTBE) and tertiary amyl methyl ether (TAME).3. The process as claimed in claim 1 , wherein said oxygenate in said hydrocarbon feed comprises at least one of methanol claim 1 , ethanol claim 1 , 1-propanol claim 1 , 2-butanol claim 1 , 1-butanol and tertiary amyl ...

PROCESS FOR CAPTURING CARBON-DIOXIDE FROM A GAS STREAM

The present disclosure relates to a process for capturing carbon-dioxide from a gas stream. In order to capture the carbon-dioxide, a support is provided and potassium carbonate (KCO) is impregnated thereon to form an adsorbent comprising potassium carbonate (KCO) impregnated support. The adsorbent is activated to form an activated adsorbent. The gas stream is passed through the adsorber to enable adsorption of the carbon-dioxide on the activated adsorbent to form a carbon-dioxide laden adsorbent. The carbon-dioxide laden adsorbent is transferred to a desorber for at least partially desorbing the carbon-dioxide from the carbon-dioxide laden adsorbent by passing a carbon-dioxide deficient stream through the desorber. The partially regenerated adsorbent is returned to the adsorber for adsorbing the carbon-dioxide from the carbon-dioxide. The process of the present disclosure reduces the overall energy demand by partially regenerating the adsorbent. 1: A process for capturing carbon-dioxide from a gas stream , said process comprising the following steps:a) providing a support, wherein said support is one of an alumina support and a silica alumina support;{'sub': 2', '3', '2', '3, 'b) impregnating potassium carbonate (KCO) on said support to form an adsorbent comprising potassium carbonate (KCO) impregnated support;'}c) activating said adsorbent in an adsorber by passing one of water-vapor and the gas stream comprising water-vapor at a temperature ranging from 40° C. to 80° C., at a pressure ranging from 1 bar to 2 bar, and for a time period ranging from 1 minute to 20 minutes to form an activated adsorbent with active adsorption sites having reduced energies;d) passing said gas stream through said adsorber containing said activated adsorbent to enable adsorption of the carbon-dioxide from said gas stream on said activated adsorbent at a temperature ranging from 40° C. to 90° C. and at a pressure ranging from 1 bar to 2 bar to form a carbon-dioxide laden adsorbent;e) ...

PROCESS AND A SYSTEM FOR PRODUCING SYNTHESIS GAS

The present disclosure relates to a process and a system for producing synthesis gas. The carbonaceous feedstock is gasified, in the presence of at least one of oxygen and steam, in a first reactor to obtain a gaseous mixture comprising H2, CO, CH4, CO2, H2O, tar and char. The gaseous mixture is treated in a second, reactor, in the presence of a catalyst, to obtain synthesis gas. The system comprises a first reactor, a connecting conduit, a second reactor, at least one cyclone separator, at least one heat exchanger and at least one synthesis gas filter unit. The process and the system of the present disclosure are capable of producing synthesis gas with comparatively higher conversion of the unreacted char. 1. A process for producing synthesis gas with increased Hto CO molar ratio from a carbonaceous feedstock , said process comprising the following steps:{'b': '100', 'sub': 2', '4', '2', '2', '2, 'gasifying said carbonaceous feedstock in a first reactor (), in the presence of at least one of oxygen and steam, at a temperature in the range of 850° C. to 1800° C. and at a pressure in the range of 1 bar to 60 bar, to obtain a gaseous mixture comprising H, CO, CH, CO, HO, tar and char where the Hto CO molar ratio is less than 1.2; and'}{'b': '300', 'sub': 2', '2, 'further gasifying said gaseous mixture in a second reactor () with at least one of steam, CO, CO and hydrogen, in the presence of a catalyst comprising alkali metal salt impregnated on silica-alumina support and, at a temperature in the range of 600° C. to 850° C. and at a pressure in the range of 1 bar to 60 bar, to obtain synthesis gas with H/CO molar ratio being in the range of 1.5 to 6.'}2. The process as claimed in claim 1 , wherein:{'b': '100', 'i. said carbonaceous feedstock is gasified in a primary zone of said first reactor () having a temperature in the range of 900° C. to 1800° C.; and'}{'b': '100', 'ii. an additional portion of said carbonaceous feedstock is gasified in a secondary zone of said ...

Method For Regeneration Of Spent Ion Exchange Resins

The present disclosure relates to a method for regeneration of spent ion exchange resins to obtain regenerated ion-exchange resins. The regenerated ion exchange resins can efficiently reduce the total acid number (TAN) of highly acidic crude oils. The present disclosure particularly relates to a method of treatment of spent ion exchange resins using at least one non-acidic crude oil condensate and at least one polar organic solvent.

METHOD FOR REMOVING CHLORIDES FROM HYDROCARBON STREAM BY STEAM STRIPPING

A method for removing chloride impurities from a heavy hydrocarbon stream is disclosed. The heavy hydrocarbon stream is contacted with a stripping medium at a temperature ranging between 100-450° C. and at a pressure ranging between 0.1-2 bar with ratio of the heavy hydrocarbon stream to the stripping medium ranging between 1-30; wherein the temperature is maintained below the initial boiling point of the hydrocarbon stream. 1. A method for removing chlorides from a heavy hydrocarbon stream , said method comprising the following steps:contacting the heavy hydrocarbon stream with a stripping medium at a temperature ranging between 100-450° C. and at a pressure ranging between 0.1-2 bar with ratio of the heavy hydrocarbon stream to the stripping medium ranging between 1-30, for stripping chlorides from the hydrocarbon stream, wherein the temperature is maintained below the initial boiling point of the hydrocarbon stream; andisolating a vapor stream containing chlorides and light hydrocarbons from the heavy hydrocarbon stream.2. The method as claimed in claim 1 , wherein the amount of chlorides present in the heavy hydrocarbon stream is in the range of 2-100 ppm.3. The method as claimed in claim 1 , wherein the heavy hydrocarbon stream contains moisture in the range of 100-2000 ppm.4. The method as claimed in claim 1 , wherein the stripping medium is steam and the chlorides are hydrolyzed to hydrogen chloride before being stripped from the hydrocarbon stream.5. The method as claimed in claim 1 , wherein the stripping medium is at least one selected from the group consisting of nitrogen claim 1 , air claim 1 , argon and any other inert gas and wherein apart from chlorides claim 1 , the stripping medium also removes moisture from the heavy hydrocarbon stream.6. The method as claimed in claim 1 , wherein the amount of light hydrocarbon present in the vapor isolated from the heavy hydrocarbon stream is less than 1 wt %.7. The method as claimed in claim 1 , wherein the ...

FCC CATALYST ADDITIVE AND A METHOD FOR ITS PREPARATION

A process for testing a zeolite based FCC catalyst and a ZSM-5 zeolite based FCC catalyst additive for simulating commercial plant yields is disclosed in, the present disclosure wherein the catalyst and the additive are subjected separately to a steaming protocol with 60 to 100% steam at a temperature in the range of 750° C. to 850° C. for 3 to 200 hours to obtain a catalyst and a catalyst additive deactivated under, said simulated commercial plant hydrothermal deactivation conditions. The deactivated catalyst and the deactivated catalyst additive are admixed in a pre-determined weight proportion. The obtained catalyst mixture is then used for cracking a hydrocarbon feed for a pre-determined period of time to generate cracking data. Product yields are measured from the generated cracking data at a pre-determined simulated commercial plant conversion of the hydrocarbon feed. 1. A process for testing a zeolite based FCC catalyst and a ZSM-5 zeolite based FCC catalyst additive for simulating commercial plant yields , said process comprising:(i) subjecting the catalyst and the additive separately to a steaming protocol with 60 to 100% steam at a temperature in the range of 750° C. to 850° C. for 3 to 200 hours characterized in that the catalyst is contacted with 60 to 100% steam, preferably 100% steam at 750° C. to 850° C., preferably 780° C. to 810° C. for 3 to 20 hours and the catalyst additive is contacted with 60 to 100% steam, preferably 100% steam at 750° C. to 850° C., preferably 780° C. to 810° C. for 3 to 200 hours;(ii) mixing the catalyst and the additive in a pre-determined proportion to obtain a catalyst mixture;(iii) injecting the catalyst mixture and a hydrocarbon feed in a micro-reactor;(iv) cracking said hydrocarbon feed with said catalyst, mixture for a pre-determined period of time to generate cracking data; and(v) measuring product yields from the generated cracking data at a pre-determined simulated commercial plant conversion of said hydrocarbon ...

A multi-compression system and process for capturing carbon dioxide

The present disclosure provides a multiple-compression system and a process for capturing carbon dioxide (CO) from a flue gas stream containing COThe disclosure also provides a process for regeneration of the carbon dioxide capture media. 1. A multi-compression process for capturing carbon dioxide (CO) from a flue gas stream containing CO; said process comprising the following steps:i. directing the flow of the flue gas stream through a first blower to obtain a pressurized flue gas stream with elevated temperature;ii. extracting the heat from the pressurized flue gas stream in a first heat exchanger using circulating thermic fluid to obtain a heated thermic fluid and a cooled pressurized flue gas stream;{'sub': '2', 'iii. directing the cooled pressurized flue gas stream to a COadsorber;'}{'sub': 2', '2, 'iv. passing in the adsorber a fluidized lean COcapture media to generate a stream comprising rich capture media and flue gas devoid of CO;'}{'sub': '2', 'v. separating in a first cyclone said rich capture media and said stream of flue gas devoid of CO;'}{'sub': '2', 'vi. directing the separated stream of flue gas devoid of COto a stack for further treatment;'}vii. leading said separated rich capture media to a second heat exchanger where it is heated to near regeneration temperature, at least partially, using said heated circulating thermic fluid to obtain a heated rich capture media;viii. feeding said heated rich capture media to a desorber;{'sub': 2', '2', '2, 'ix. heating the heated rich capture media in the desorber with the help of circulating heated non-thermic fluid to desorb COfrom the heated rich capture media to generate hot lean capture media and COgas and optionally using a part of the generated COgas for fluidization of the heated rich capture media in the desorber;'}{'sub': '2', 'x. separating COgas from the hot and lean capture media;'}xi. circulating the heated non-thermic fluid through the desorber by the thermosyphon principle by heating the non- ...

Single compression system and process for capturing carbon dioxide

The present disclosure provides a single compression system and a process for capturing carbon dioxide (CO 2 ) from a flue gas stream containing CO 2 The disclosure also provides a process for regeneration of the carbon dioxide capture media.

PROCESS FOR CATALYTIC CONVERSION OF LOW VALUE HYDROCARBON STREAMS TO LIGHT OLEFINS

A process for catalytic conversion of low value hydrocarbon streams to light olefins in comparatively higher yields is disclosed. Propylene is obtained in amounts higher than 20 wt. % and ethylene higher than 6 wt. %. The process is carried out in a preheated cracking reactor having a single riser and circulating an FCC catalyst. The riser is divided into three temperature zones in which different hydrocarbon feeds are introduced. An oxygenate feed is introduced in the operative top zone in the riser. Heat for the endothermic cracking is obtained by the exothermic reaction of converting the oxygenate feed into gas and/or from a regenerator in which the spent FCC catalyst is burnt. 1. A process for obtaining light olefins with comparatively higher yields comprising the following steps:i. providing a pre-heated cracking reactor having a riser maintained at a pressure in the range of 0.5 to 3 bar, charged with a solid acidic FCC catalyst, said riser being provided with at least three temperature zones; a first zone operative at the bottom of the riser having a temperature varying between 650° C. to 750° C., a second intermediate zone having a temperature varying between 580° C. to 650° C. operative above the first zone and a third zone operative at the top of the riser having a temperature in the range of from 500° C. to 620° C.;ii. feeding, at a weight hourly space velocity of 0.2 h-1 to 50 h-1, a first hydrocarbon feed having C4 hydrocarbons and other paraffinic streams to the first zone, feeding at a weight hourly space velocity of 5 h-1 to 100 h-1, a second hydrocarbon feed having olefinic naphtha stream to the second zone and feeding, at a weight hourly space velocity of 40 h-1 to 200 h-1, a third hydrocarbon feed comprising heavy hydrocarbons to the third zone; andiii. cracking the first, second and third hydrocarbon feeds sequentially, with the help of heat generated by at least one of two heat generating reactions selected from the group consisting of (a) ...

A PROCESS FOR CATALYTIC GASIFICATION OF CARBONACEOUS FEEDSTOCK

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support iand heat carrier in the gasification zone (). The gasification zone () is operated at 700-750° C. to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably KCO, so that conversion proportional to total KCOto solid carbon ratio is achieved with as high KCOloading as 50 wt % on the solid support. The combustion zone () is operated at 800°-840° C., to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles. 1. A process for catalytic gasification of a carbonaceous feedstock to synthesis gas , said process comprising the following steps:{'b': 102', '202, 'i. gasifying a primary portion of said carbonaceous feedstock in a fluidized gasification zone (, ) at a temperature between 600-800° C. with steam and in the presence of an alkali metal catalyst impregnated on a solid particulate carrier, to produce synthesis gas; wherein heat for the endothermic gasification reaction is supplied by heated solid particulate carrier provided in said gasification zone at a carrier to feedstock ratio of 10 to 50;'}{'b': 102', '202, 'ii. discharging heat-extracted solid particulate carrier impregnated with said alkali metal catalyst from the operative top of the fluidized gasification zone (, ); and'}{'b': 140', '240, 'iii. combusting a secondary portion of said carbonaceous feedstock and unreacted carbon from said gasification zone in a fluidized combustion zone (, ) at a temperature between 800-840° C. with air, wherein heat generated during the exothermic combustion reaction is transferred to said heat-extracted solid particulate carrier to provide said heated solid ...

A process for the removal of sodium from di-sulfide oil

In the present disclosure there is provided a process for obtaining di-sulfide oil having sodium level below 0.1 ppm wherein a stream comprising di-sulfide oil having sodium level 1 ppm, collected as a waste stream from LPG desulfurization unit, is passed through an alumina bed packed in a column at a pre-determined liquid hourly space velocity (LHSV) and at pre-determined temperature to obtain a treated stream comprising di-sulfide oil having sodium level below 0.1 ppm.

PROCESS FOR PROPYLENE AND LPG RECOVERY IN FCC FUEL GAS

The present invention provides a process for recovery of propylene and LPG from the fuel gas produced in FCC unit by contacting a heavier hydrocarbon feed with FCC catalyst. The process provides an energy efficient configuration for revamping an existing unit constrained on wet gas compressor capacity or for designing a new gas concentration unit to recover propylene and LPG recovery beyond 97 mole %. The process of the present invention provides an increase propylene and LPG recovery without loading wet gas compressor with marginal increase in liquid loads. 2. The process as claimed in claim 1 , wherein the main fractionator overhead condenser pressure is from 10 psig and above claim 1 , preferably 25 psig and above.3. The process as claimed in claim 1 , wherein the debutanized naphtha is supplied to the absorber at temperature preferably between from about 20° C. to about 30° C. using chilled water as an indirect cooling media.4. The process as claimed in claim 1 , wherein the gaseous fraction from the absorber is optionally further treated before leaving the FCC gas concentration section as fuel gas.5. The process for the recovery of propylene and LPG from a product mixture obtained by contacting a hydrocarbon feed with a catalyst in a FCC process substantially as herein described with reference to the foregoing examples and of the accompanying drawings.6. The process as claimed in claim 2 , wherein the debutanized naphtha is supplied to the absorber at temperature preferably between from about 20° C. to about 30° C. using chilled water as an indirect cooling media.7. The process as claimed in claim 2 , wherein the gaseous fraction from the absorber is optionally further treated before leaving the FCC gas concentration section as fuel gas.8. The process as claimed in claim 3 , wherein the gaseous fraction from the absorber is optionally further treated before leaving the FCC gas concentration section as fuel gas. Present invention provides process for the ...

PROCESS FOR RECOVERING VANADIUM IN THE FORM OF IRON VANADATE FROM A GASIFIER SLAG

The present disclosure relates to a process for recovering vanadium in the form of iron vanadate from a gasifier slag. The process comprises pulverizing the slag to obtain pulverized slag (). The pulverized slag () is soaked in water () and an alkali salt () to obtain a slurry (), followed by roasting the slurry in the presence of air to obtain roasted slag () which is leached () to obtain a first solution (). The first solution () is heated at a temperature in the range of 60° C. to 80° C. while adding an iron salt () in an amount in the range of 10 wt % to 60 wt % at a pH in the range of 4 to 10, to obtain a second solid residue () which is dried to obtain iron vanadate (). 1. A process for recovering vanadium in the form of iron vanadate from a gasifier slag , said process comprising the following steps:a) pulverizing gasifier slag to a particle size less than 100 μm to obtain pulverized slag;b) soaking said pulverized slag in water and alkali salt to obtain a slurry;c) roasting said slurry in the presence of air at a temperature in the range of 750° C. to 1100° C. to obtain roasted slag;d) leaching said roasted slag in water heated to a temperature below its boiling point to obtain a first biphasic mixture comprising a first solid phase and a first liquid phase;e) filtering said first biphasic mixture to obtain a first solid residue and a first solution comprising vanadium compounds;f) heating said first solution to a temperature in the range of 60° C. to 80° C. while adding therein, an iron salt in an amount in the range of 10 wt % to 60 wt % at a pH in the range of 4 to 10, to obtain a second biphasic mixture comprising a second solid phase and a second liquid phase;g) filtering said second biphasic mixture to obtain a second solid residue comprising iron vanadate and a second solution comprising said alkali salt; andh) drying said second solid residue at a temperature in the range of 300° C. to 500° C. to obtain iron vanadate.2. The process as claimed in ...

Upgradation of undesirable olefinic liquid hydrocarbon streams

A process for converting undesirable olefinic hydrocarbon streams to hydrogen and petrochemical feedstock e.g. light olefins in C 2 -C 4 range and aromatics especially toluene and xylenes, which comprises simultaneous cracking and reforming at olefin rich hydrocarbons using a catalyst consisting of dehydrogenating metal components, shape selective zeolite components and large pore acidic components in different proportions in a circulating fluidized bed reactor-regenerator system having reactor temperature within 450-750° C. and WHSV of 0.1-60 hour -1 .

catalyst additive and method of preparation thereof

Fluid catalytic cracking (FCC) process for manufacturing propylene and ethylene in increased yield

Manufacture of propylene and ethylene in a FCC unit. Each FCC riser comprises an acceleration zone, a lift stream feed nozzle, a main hydrocarbon stock feed nozzle, and an olefinic naphtha feed nozzle. Mixed FCC catalyst comprising at least 2 percent by weight pentasil zeolite and at least 10 percent by weight Y-zeolite is injected at the bottom of each FCC riser. Olefinic naptha is injected through the olefinic feed nozzle, main hydrocarbon stock is injected through the main hydrocarbon stock feed nozzle and lift stream is injected through the lift stream feed nozzle. Lift stream comprises olefinic C 4 hydrocarbon stream and optionally steam and/or a fuel gas. Olefinic C 4 hydrocarbon steam is cracked in the acceleration zone at 600 to 800° C., 0.8 to 5 kg/cm 2 (gauge) pressure, WHSV 0.2 to 100 hr up 1 and vapour residence time 0.2 to 5 seconds.

An improved process for recovery of propylene and lpg from fcc fuel gas using stripped main column overhead distillate as absorber oil

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support and heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

Process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support i and heat carrier in the gasification zone ( 102 ). The gasification zone ( 102 ) is operated at 700-750° C. to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt % on the solid support. The combustion zone ( 140 ) is operated at 800°-840° C., to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

Hydrothermally stable catalyst composition and a process for preparation thereof

The present disclosure relates to a hydrothermally stable catalyst composition. The hydrothermally stable supported catalyst composition comprises K 2 CO 3 impregnated on an amorphous silica-alumina support. The weight ratio of silica to alumina in the support is in the range of 0.1 to 1.5. The amount of K 2 CO 3 is in the range of 5 wt % to 60 wt % with respect to the total catalyst composition. The catalyst composition is characterized by a pore volume in the range of 0.1 cc/g to 0.9 cc/g, a surface area in the range of 40 m 2 /g to 250 m 2 /g and an attrition index in the range of 2% to 8%. The present disclosure also relates to a process for preparing the catalyst composition. The catalyst composition provides improved hydrothermal stability, attrition resistance, high pore volume and surface area for gasifying carbonaceous feed at low temperature, as compared to a conventional catalyst composition.

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support and heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

A process and a system for producing synthesis gas

The present disclosure relates to a process and a system for producing synthesis gas. The carbonaceous feedstock is gasified, in the presence of at least one of oxygen and steam, in a first reactor to obtain a gaseous mixture comprising H

Multi-compression system and process for capturing carbon dioxide

The present disclosure provides a multiple-compression system and a process for capturing carbon dioxide (CO 2 ) from a flue gas stream containing CO 2 . The disclosure also provides a process for regeneration of the carbon dioxide capture media.

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses .gamma.-alumina as a catalyst support iand heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of .gamma.-alumina to .alpha.-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K2CO3, so that conversion proportional to total K2CO3 to solid carbon ratio is achieved with as high K2CO3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the .gamma.-alumina to a-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

A process for catalytic conversion of low value hydrocarbon streams to light olefins

A process for catalytic conversion of low value hydrocarbon streams to light olefins in comparatively higher yields is disclosed. Propylene is obtained in amounts higher than 20 wt. % and ethylene higher than 6 wt. %. The process is carried out in a preheated cracking reactor having a single riser and circulating an FCC catalyst. The riser is divided into three temperature zones in which different hydrocarbon feeds are introduced. An oxygenate feed is introduced in the operative top zone in the riser. Heat for the endothermic cracking is obtained by the exothermic reaction of converting the oxygenate feed into gas and / or from a regenerator in which the spent FCC catalyst is burnt.

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support iand heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the γ-alumina to a-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

A method for catalytic conversion of waste plastic into liquid fuel

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses .gamma.-alumina as a catalyst support iand heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of .gamma.-alumina to .alpha.-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K2CO3, so that conversion proportional to total K2CO3 to solid carbon ratio is achieved with as high K2CO3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the .gamma.-alumina to a-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

A process for catalytic conversion of low value hydrocarbon streams to light olefins

A process for catalytic conversion of low value hydrocarbon streams to light olefins in comparatively higher yields is disclosed. Propylene is obtained in amounts higher than 20 wt. % and ethylene higher than 6 wt. %. The process is carried out in a preheated cracking reactor having a single riser and circulating an FCC catalyst. The riser is divided into three temperature zones in which different hydrocarbon feeds are introduced. An oxygenate feed is introduced in the operative top zone in the riser. Heat for the endothermic cracking is obtained by the exothermic reaction of converting the oxygenate feed into gas and / or from a regenerator in which the spent FCC catalyst is burnt.

Fluidized catalytic cracking process and apparatus

A fluidized catalytic cracking apparatus includes a riser containing a regenerated catalyst and adsorbant, and has a first inlet for introduction of high velocity steam, a second inlet for introduction of a feed stream containing heavy residual fractions with high concentrations of conradson coke, metals including vanadium and nickel, and additional poisons including nitrogen, a third inlet for introduction of an adsorbent, and a fourth inlet disposed above the third inlet means for introduction of a regenerated catalyst, the adsorbent having a particle size which is larger than that of the regenerated catalyst. A stripper is provided into which the riser extends for causing separation of a hydrocarbon fraction from spent catalyst and adsorbent, and a separator is connected to the stripper and has a base, an inlet at the base for introduction of steam in the upward direction so as to provide a transport velocity in the upward direction for the spent catalyst and cause a separation of the particles of the spent catalyst from the adsorbent in use. A regenerator is connected to the separator and has an outlet and is in flow communication with the fourth inlet for introduction of the regenerated catalyst into the riser. A burner is provided for receiving the adsorbent from the separator and for causing a regeneration thereof, the burner having an inlet for introduction of oxygen containing gas and an outlet in flow communication with the third inlet for introduction of the adsorbent into the riser. A lift line is connected between the separator and the regenerator for allowing a flow of the spent catalyst from the separator into the regenerator while leaving the adsorbent within the separator in a fluidized condition the lift line having a plurality of steam inlets disposed at different elevations along its length for introduction of steam to provide said transport velocity.

A multi stage selective catalytic cracking process and a system for producing high yield of middle distillate products from heavy hydrocarbon feedstocks

An fcc catalyst composition and a process for its preparation

The present disclosure relates to an FCC catalyst composition and a process for its preparation. The FCC catalyst composition comprises Y type zeolite, silicon oxide, alumina, at least one clay, at least one rare earth metal, and at least one metal oxide. The FCC catalyst composition of the present disclosure provides improved yields of high value gasoline such as propylene and LPG and reduces yields of low value hydrocarbons such as CSO and LCO.

A hydrothermally stable catalyst composition and a process for preparation thereof

The present disclosure relates to a hydrothermally stable catalyst composition. The hydrothermally stable supported catalyst composition comprises K

A process for catalytic conversion of low value hydrocarbon streams to light olefins

A process for catalytic conversion of low value hydrocarbon streams to light olefins in comparatively higher yields is disclosed. Propylene is obtained in amounts higher than 20 wt. % and ethylene higher than 6 wt. %. The process is carried out in a preheated cracking reactor having a single riser and circulating an FCC catalyst. The riser is divided into three temperature zones in which different hydrocarbon feeds are introduced. An oxygenate feed is introduced in the operative top zone in the riser. Heat for the endothermic cracking is obtained by the exothermic reaction of converting the oxygenate feed into gas and / or from a regenerator in which the spent FCC catalyst is burnt.

A process for catalytic gasification of carbonaceous feedstock

公開了一種旨在雙流化床式反應器中生產合成氣體之催化氣化一種含碳原料之改善的工藝。此工藝在氣化區域(102)中使用γ-氧化鋁作為一種催化劑輔料及熱載體。氣化區域(102)運行於700至750℃下，旨在預防γ-氧化鋁大量轉化成α-氧化鋁，由此實現高催化劑載入及高再迴圈率。催化劑是一種鹼金屬，首選K2CO3，以此達成轉化率與K2CO3對固體碳料之比率成正比，且高達50%重量比之K2CO3載入於固體輔料上。燃燒區域(140)運行於800至840℃下，旨在預防任何γ-氧化鋁大量轉化成α-氧化鋁，並使在兩次連續迴圈之間的催化劑再迴圈率達98%。

Method for removing chlorides from hydrocarbon stream by steam stripping

A method for removing chloride impurities from a heavy hydrocarbon stream is disclosed. The heavy hydrocarbon stream is contacted with a stripping medium at a temperature ranging between 100-450° C. and at a pressure ranging between 0.1-2 bar with ratio of the heavy hydrocarbon stream to the stripping medium ranging between 1-30; wherein the temperature is maintained below the initial boiling point of the hydrocarbon stream.

A process for catalytic conversion of low value hydrocarbon streams to light olefins

A process for catalytic conversion of low value hydrocarbon streams to light olefins in comparatively higher yields is disclosed. Propylene is obtained in amounts higher than 20 wt. % and ethylene higher than 6 wt. %. The process is carried out in a preheated cracking reactor having a single riser and circulating an FCC catalyst. The riser is divided into three temperature zones in which different hydrocarbon feeds are introduced. An oxygenate feed is introduced in the operative top zone in the riser. Heat for the endothermic cracking is obtained by the exothermic reaction of converting the oxygenate feed into gas and / or from a regenerator in which the spent FCC catalyst is burnt.

A hydrothermally stable catalyst composition and a process for preparation thereof

The present disclosure relates to a hydrothermally stable catalyst composition. The hydrothermally stable supported catalyst composition comprises K

The upgradation of undesirable olefinic liquid hydrocarbon streams

A process for converting undesirable olefinic hydrocarbon streams to hydrogen and petrochemical feedstock e.g. light olefins in C2-C4 range and aromatics especially toluene and xylenes, which comprises simultaneous cracking and reforming of olefin rich hydrocarbons using a catalyst consisting of dehydrogenating metal components, shape selective zeolite components and large pore acidic components in different proportions in a circulating fluidized bed reactor-regenerator system having reactor temperature within 450-750°C and WHSV of 0.1-60 hour-1.

A process for capturing carbon-dioxide from a gas stream

The present disclosure relates to a process for capturing carbon-dioxide from a gas stream. In order to capture the carbon-dioxide, a support is provided and potassium carbonate (K 2 CO 3 ) is impregnated thereon to form an adsorbent comprising potassium carbonate (K 2 CO 3 ) impregnated support. The adsorbent is activated to form an activated adsorbent. The gas stream is passed through the adsorber to enable adsorption of the carbon-dioxide on the activated adsorbent to form a carbon-dioxide laden adsorbent. The carbon-dioxide laden adsorbent is transferred to a desorber for at least partially desorbing the carbon-dioxide from the carbon-dioxide laden adsorbent by passing a carbon-dioxide deficient stream through the desorber. The partially regenerated adsorbent is returned to the adsorber for adsorbing the carbon-dioxide from the carbon-dioxide. The process of the present disclosure reduces the overall energy demand by partially regenerating the adsorbent.

Method for catalytic conversion of waste plastic into liquid fuel

The present disclosure provides a method for catalytic conversion of waste plastic into liquid fuel. The method comprises thermally decomposing the waste plastic at a temperature in the range of 350 to 650° C. and under a pressure in the range of 0.0010 psi to 0.030 psi, to obtain a gaseous stream. The gaseous stream is further subjected to four stage sequential cooling to a temperature in the range of −5 to −15° C. to obtain a gas-liquid mixture comprising a gaseous fraction and a liquid fraction. The gas-liquid mixture is fed to the gas-liquid separator to obtain the gaseous fraction comprising C1 to C4 hydrocarbons and the liquid fraction comprising liquid fuel. The method of the present disclosure is simple, economical and energy efficient, which provides a high value liquid fuel with enhanced yield.

A hydrothermally stable catalyst composition and a process for preparation thereof

The present disclosure relates to a hydrothermally stable catalyst composition. The hydrothermally stable supported catalyst composition comprises K 2 CO 3 impregnated on an amorphous silica-alumina support. The weight ratio of silica to alumina in the support is in the range of 0.1 to 1.5. The amount of K 2 CO 3 is in the range of 5 wt% to 60 wt% with respect to the total catalyst composition. The catalyst composition is characterized by a pore volume in the range of 0.1 cc/g to 0.9 cc/g, a surface area in the range of 40 m 2 /g to 250 m 2 /g and an attrition index in the range of 2 % to 8 %. The present disclosure also relates to a process for preparing the catalyst composition. The catalyst composition provides improved hydrothermal stability, attrition resistance, high pore volume and surface area for gasifying carbonaceous feed at low temperature, as compared to a conventional catalyst composition.

Processo de recuperação de vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador

a presente divulgação refere-se a um processo para recuperar vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador. o processo compreende pulverizar a escória para obter a escória pulverizada (2). a escória pulverizada (2) é imergida em água (6) e em um sal alcalino (4) para obter uma pasta (8), seguida de torrefação da pasta na presença de ar para obter a escória torrada (12) que é lixiviada (14) para obter uma primeira solução (18). a primeira solução (18) é aquecida a uma temperatura na faixa de 60ºc a 80ºc, enquanto se adiciona um sal de ferro (17) em uma quantidade na faixa de 10% em peso a 60% em peso a um ph na faixa de 4 a 10, para se obter um segundo resíduo sólido (21), que é seco para se obter vanadato de ferro (24).

An fcc catalyst composition and a process for its preparation

An fcc catalyst composition and a process for its preparation

Process for recovering vanadium in the form of iron vanadate from a gasifier slag

The present disclosure relates to a process for recovering vanadium in the form of iron vanadate from a gasifier slag. The process comprises pulverizing the slag to obtain pulverized slag (2). The pulverized slag (2) is soaked in water (6) and an alkali salt (4) to obtain a slurry (8), followed by roasting the slurry in the presence of air to obtain roasted slag (12) which is leached (14) to obtain a first solution (18). The first solution (18) is heated at a temperature in the range of 60° C. to 80° C. while adding an iron salt (17) in an amount in the range of 10 wt % to 60 wt % at a pH in the range of 4 to 10, to obtain a second solid residue (21) which is dried to obtain iron vanadate (24).

A process for the production of needle coke

The present disclosure relates to a process for the production of needle coke in a delayed coker plant. The needle coke so obtained by the process of the present disclosure has a co-efficient of thermal expansion (CTE) of less than 1.2 x 10 -6 /°C. The process of the present disclosure eliminates the step of hydrotreating of the first feed and second feed for the production of good quality coke. The process of the present disclosure maximizes the production of the needle coke having low CTE and low sulfur content in the delayed coker coke drum.

A continuous process for the synthesis of dimethyl carbonate over a cerium-based catalyst formulation

The present invention discloses a continuous process for the synthesis of dimethyl carbonate from methanol and carbon dioxide over a ceria-based mixed metal oxide-silica catalyst formulation in the presence of a dehydrating or water trapping compound (2-Cyanopyridine).

A method for regeneration of spent ion exchange resins

Process and composition of catalyst/ additive for reducing fuel gas yield in fluid catalytic cracking (fcc) process

Provided is a process for cracking of high boiling petroleum feedstock and the catalyst therein and the preparation of the catalyst, said catalyst comprising (a) a FCC catalyst component and (b) an additive component, wherein each of said components independently contain zeolite (5-60wt%), clay (10-40wt%), binder (0-40wt%), alkaline earth metal (0.01-2.0wt%). The catalyst is used in cracking of hydrocarbon feedstock containing hydrocarbons of higher molecular weight and higher boiling point for producing lower yield of fuel gas without effecting the conversion and yield of general cracking products such as gasoline, propylene and C 4 olefins.

Processo para obter óxido de vanádio a partir de uma escória de gaseificador

PROCESSO PARA OBTER ÓXIDO DE VANÁDIO A PARTIR DE UMA ESCÓRIA DE GASEIFICADOR. É divulgado um processo para obter componente de vanádio na forma de óxido de vanádio a partir de escória de gaseificador. O processo compreende pulverizar a escória para obter escória pulverizada, que é misturada com água e um sal alcalino para obter uma pasta. A pasta é seca e depois torrada na presença de ar para obter uma escória torrada. A escória torrada é lixiviada para se obter um primeiro filtrado compreendendo o componente de vanádio. O primeiro filtrado reage com um sal de magnésio para remover um componente de sílica na forma de um precipitado. O segundo filtrado livre de sílica reage com um sal de amônio para obter metavanadato de amônio, que é posteriormente calcinado para se obter uma quantidade significativa de pentóxido de vanádio (V2O5).

Processo de recuperação de vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador

A presente divulgação refere-se a um processo para recuperar vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador. O processo compreende pulverizar a escória para obter a escória pulverizada (2). A escória pulverizada (2) é imergida em água (6) e em um sal alcalino (4) para obter uma pasta (8), seguida de torrefação da pasta na presença de ar para obter a escória torrada (12) que é lixiviada (14) para obter uma primeira solução (18). A primeira solução (18) é aquecida a uma temperatura na faixa de 60°C a 80°C, enquanto se adiciona um sal de ferro (17) em uma quantidade na faixa de 10% em peso a 60% em peso a um pH na faixa de 4 a 10, para se obter um segundo resíduo sólido (21), que é seco para se obter vanadato de ferro (24).

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A process for the removal of sodium from di-sulfide oil

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A process for the removal of sodium from di-sulfide oil

In the present disclosure there is provided a process for obtaining di-sulfide oil having sodium level below 0.1 ppm wherein a stream comprising di-sulfide oil having sodium level 1 ppm, collected as a waste stream from LPG desulfurization unit, is passed through an alumina bed packed in a column at a pre-determined liquid hourly space velocity (LHSV) and at pre-determined temperature to obtain a treated stream comprising di-sulfide oil having sodium level below 0.1 ppm.

Aditivo de catalizador para craqueo catalítico fluido y su proceso de preparación

La presente se relaciona con un aditivo de catalizador de CCF, que contiene una ceolita, un ligante y una arcilla, donde el contenido de fósforo está en forma de P₂O₅ y sílice coloidal como ligante. El aditivo de catalizador de CCF está caracterizado por la ausencia de la fase de cristal de fosfato de aluminio y la presencia de al menos una de las especies de aluminio tetraédrico de estructura de ceolita, aluminio tetraédrico distorsionado de estructura de ceolita y aluminio octaédrico sin estructura. La presente también se relaciona con un proceso para la preparación de dicho aditivo de catalizador de CCF.

Process for obtaining vanadium oxide from a gasifier slag field

A process for obtaining vanadium component in the form of vanadium oxide from gasifier slag is disclosed. The process comprises pulverizing the slag to obtain pulverized slag, which is blended with water and an alkali salt to obtain a slurry. The slurry is dried and then roasted in the presence of air to obtain a roasted slag. The roasted slag is leached to obtain a first filtrate comprising the vanadium component. The first filtrate is reacted with a magnesium salt to remove a silica component in the form of a precipitate. The silica free second filtrate is reacted with an ammonium salt to obtain ammonium metavanadate, which is further calcined to obtain the significant amount of vanadium pentoxide (V2O5).

Un procedimiento para la conversión catalítica de residuos de plástico en combustible líquido

La presente divulgación proporciona un método para la conversión catalítica de residuos de plástico en combustible líquido. El método comprende descomponer térmicamente el plástico de desecho a una temperatura en el rango de 350 a 650 °C y bajo una presión en el rango de 0,0010 psi a 0,030 psi, para obtener una corriente gaseosa. La corriente gaseosa se somete además a un enfriamiento secuencial de cuatro etapas a una temperatura en el intervalo de -5 a -15ºC para obtener una mezcla gas-líquido que comprende una fracción gaseosa y una fracción líquida. La mezcla gas-líquido se alimenta al separador gas-líquido para obtener la fracción gaseosa que comprende hidrocarburos C1 a C4 y la fracción líquida que comprende combustible líquido. El método de la presente divulgación es simple, económico y eficiente desde el punto de vista energético, lo que proporciona un combustible líquido de alto valor con un rendimiento mejorado. (Traducción automática con Google Translate, sin valor legal)

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Continuous process for the synthesis of dimethyl carbonate over a cerium-based catalyst formulation

The present invention discloses a continuous process for the synthesis of dimethyl carbonate from methanol and carbon dioxide over a ceria-based mixed metal oxide-silica catalyst formulation in the presence of a dehydrating or water trapping compound (2-Cyanopyridine).

Process for obtaining vanadium oxide from a gasifier slag

Verfahren zur Herstellung von LPG und Leichtolefinen mit hohen Ausbeuten

Process for reducing the amount of carbon disulphide (cs 2) in a hydrocarbon feed

The present disclosure relates to a process for reducing the amount of carbon disulphide (CS 2 ) in a hydrocarbon feed containing C 5 -C 8 fractions. The hydrocarbon feed is treated with an amine functionalized anion exchange resin (basic anion exchange resin) to obtain a mixture comprising a liquid fraction containing treated hydrocarbon and a solid mass containing an adduct of CS 2 and the amine functionalized anion exchange resin. The so obtained liquid fraction containing the treated hydrocarbon is separated from the solid mass to obtain the hydrocarbon having CS 2 content less than 2 ppm. The amine functionalized anion exchange resin can be regenerated from the solid mass.

Procedimiento para la produccion con elevado rendimiento de lpg y olefinas ligeras.

LA INVENCION SE REFIERE A UN PROCESO PARA EL CRAQUEO CATALITICO DE MATERIAL DE ALIMENTACION A BASE DE PETROLEO, PARA PRODUCIR GLP DE GRAN RENDIMIENTO Y OLEFINAS LIGERAS CON C 3 Y C 4 , EN PRESENCIA DE UN CATALIZADOR ACIDO SOLIDO Y COMPONENTES ACIDOS CON IMPORTANTES TAMAÑOS DE POROS EN UN REACTOR DE LECHO FLUIDIFICADO. EL REACTOR ACTUA EN LA GAMA DE 40 A 120 H -1 A LA VELOCIDAD ESPACIAL HORARIA EN PESO, CON UNA RELACION CATALIZADOR/PETROLEO DE 15/25 Y UNA TEMPERATURA DE SUBIDA DE 520 - 600°C.

FCC catalyst composition and a process for its preparation

The present disclosure relates to an FCC catalyst composition and a process for preparing the same. In a first aspect, there is provided an FCC catalyst composition comprising 25 to 45 wt % Y-type zeolite, 20 to 40 wt % silicon oxide, 5 to 25 wt % alumina, 5 to 35 wt % of at least one clay and 0.5 to 3 wt % of at least one rare earth oxide. The weight % of each of the component is with respect to the total weight of the composition. The FCC catalyst composition has an average particle size in the range of 45-120μ. In a second aspect, there is provided a process for preparing the FCC catalyst composition, which uses ball milled pseudoboehmite having an average particle size in the range of 1 to 8 micron and the whole process is carried out at a pH value in the range of 6 to 7.

System and method for preparing hydrocarbon blend from multiple component streams

A computer implemented blend control system and method for preparation of a hydrocarbon blend from a plurality of components drawn from respective component tanks have been disclosed. The system, in accordance with the present disclosure includes at least one sensor and analyzer adapted to sense and analyze a first attribute of at least one of the components for obtaining first attribute data. The system further includes, at least one optimizer having a data storage means for storing attribute based model data. The optimizer receives the first attribute data and transmits the received first attribute data to a comparator which computes an optimized proportion data between each of the component streams to enable selective drawing of each of the component streams in accordance with the optimized proportion data for preparing the hydrocarbon blend.

Computer implemented blend control system and method for preparation of a hydrocarbon blend

A computer implemented blend control system and method for preparation of a hydrocarbon blend from a plurality of component streams have been disclosed. The system includes a product tank for receiving a mixture comprising the plurality of component streams. The system further includes a sensor and analyzer adapted to sense and analyze a first attribute of the received mixture for obtaining a first attribute data. The system further includes an optimizer which stores the attribute based model data, receives the first attribute data and compares the received first attribute data with the attribute based model data to compute an optimized proportion data, based on which the component streams are selectively drawn into the product tank for preparing the hydrocarbon blend.

Method for regeneration of spent ion exchange resins

The present disclosure relates to a method for regeneration of spent ion exchange resins to obtain regenerated ion-exchange resins. The regenerated ion exchange resins can efficiently reduce the total acid number (TAN) of highly acidic crude oils. The present disclosure particularly relates to a method of treatment of spent ion exchange resins using at least one non-acidic crude oil condensate and at least one polar organic solvent.

Process for the removal of sodium from di-sulfide oil

In the present disclosure there is provided a process for obtaining di-sulfide oil having sodium level below 0.1 ppm wherein a stream comprising di-sulfide oil having sodium level 1 ppm, collected as a waste stream from LPG desulfurization unit, is passed through an alumina bed packed in a column at a pre-determined liquid hourly space velocity (LHSV) and at pre-determined temperature to obtain a treated stream comprising di-sulfide oil having sodium level below 0.1 ppm.

Process and composition of catalyst/additive for reducing fuel gas yield in fluid catalytic cracking (FCC) process

The present invention relates to a catalyst composition for Fluid Catalytic Cracking (FCC) which contains a combination of a FCC catalyst component and an additive component with certain physical properties attributed therein. The present invention is also directed to provide methods for the preparation of the catalyst composition for FCC. The admixture of the FCC catalyst component and additive component is used in cracking of hydrocarbon feedstock containing hydrocarbons of higher molecular weight and higher boiling point and/or olefin gasoline naphtha feedstock for producing lower yield of fuel gas without affecting the conversion and yield of general cracking products such as gasoline, propylene and C 4 olefins.

Process for catalytic conversion of low value hydrocarbon streams to light olefins

A process for catalytic conversion of low value hydrocarbon streams to light olefins in comparatively higher yields is disclosed. Propylene is obtained in amounts higher than 20 wt. % and ethylene higher than 6 wt. %. The process is carried out in a preheated cracking reactor having a single riser and circulating an FCC catalyst. The riser is divided into three temperature zones in which different hydrocarbon feeds are introduced. An oxygenate feed is introduced in the operative top zone in the riser. Heat for the endothermic cracking is obtained by the exothermic reaction of converting the oxygenate feed into gas and/or from a regenerator in which the spent FCC catalyst is burnt.