US20150136660A1 - Process for removing a contaminant from coal tar - Google Patents
Process for removing a contaminant from coal tar Download PDFInfo
- Publication number
- US20150136660A1 US20150136660A1 US14/472,263 US201414472263A US2015136660A1 US 20150136660 A1 US20150136660 A1 US 20150136660A1 US 201414472263 A US201414472263 A US 201414472263A US 2015136660 A1 US2015136660 A1 US 2015136660A1
- Authority
- US
- United States
- Prior art keywords
- blocks
- contaminant
- coal tar
- supercritical
- extraction agent
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/02—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/18—Working-up tar by extraction with selective solvents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/20—Refining by chemical means inorganic or organic compounds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/14—Hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
- C10G21/12—Organic compounds only
- C10G21/16—Oxygen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/003—Specific sorbent material, not covered by C10G25/02 or C10G25/03
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
- C10G25/03—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material with crystalline alumino-silicates, e.g. molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
- C10G57/005—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with alkylation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including a sorption process as the refining step in the absence of hydrogen
Definitions
- Coke Pyrolysis of coal produces coke and coal tar.
- the coke-making or “coking” process consists of heating the material in closed vessels in the absence of oxygen to very high temperatures.
- Coke is a porous but hard residue that is mostly carbon and inorganic ash, which is used in making steel.
- Coal tar is the volatile material that is driven off during heating, and it comprises a mixture of a number of hydrocarbon compounds. It can be separated to yield a variety of organic compounds, such as benzene, toluene, xylene, naphthalene, anthracene, and phenanthrene. These organic compounds can be used to make numerous products, for example, dyes, drugs, explosives, flavorings, perfumes, preservatives, synthetic resins, and paints and stains but may also be processed into fuels and petrochemical intermediates. The residual pitch left from the separation is used for paving, roofing, waterproofing, and insulation.
- Coal tar has a number of contaminants that need to be removed, such as nitrogen, oxygen, or sulfur-containing compounds.
- One aspect of the invention is a process for removing at least one product from coal tar.
- the process includes providing at least a portion of a coal tar stream; removing at least one contaminant from the at least the portion of the coal tar stream by extraction with an extraction agent or adsorption with an adsorbent to form a treated coal tar stream having a reduced level of the at least one contaminant, the extraction agent comprising at least one of amphiphilic block copolymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, cyclodextrins, functionalized cyclodextrins, and cyclodextrin-functionalized polymers, the adsorbent comprising exfoliated graphite oxide, thermally exfoliated graphite oxide or intercalated graphite compounds, and the at least one contaminant comprising nitrogen heterocyclic aromatics, oxygen heterocyclic aromatics, and sulfur heterocyclic aromatics; and separating the at least the portion of the coal
- the FIGURE is an illustration of one embodiment of the process of the present invention.
- the FIGURE shows one embodiment of a coal conversion process 5 .
- the coal feed 10 can be sent to the pyrolysis zone 15 , the gasification zone 20 , or the coal feed 10 can be split into two parts and sent to both.
- the coal is heated at high temperature, e.g., up to about 2,000° C. (3600° F.), in the absence of oxygen to drive off the volatile components. Coking produces a coke stream 25 and a coal tar stream 30 .
- the coke stream 25 can be used in other processes, such as the manufacture of steel.
- the coal tar stream 30 which comprises the volatile components from the coking process can be sent to an optional contaminant removal zone 35 , if desired.
- the contaminant removal zone 35 for removing one or more contaminants from the coal tar stream or another process stream may be located at various positions along the process depending on the impact of the particular contaminant on the product or process and the reason for the contaminant's removal, as described further below.
- the contaminant removal zone 35 can be positioned upstream of the separation zone 45 , as shown in the FIGURE.
- Some contaminants have been identified to interfere with a downstream processing step or hydrocarbon conversion process, in which case the contaminant removal zone 35 may be positioned upstream of the separation zone 45 or between the separation zone 45 and the particular downstream processing step at issue. Still other contaminants have been identified that should be removed to meet particular product specifications.
- contaminant removal zones may be positioned at different locations along the process.
- a contaminant removal zone may overlap or be integrated with another process within the system, in which case the contaminant may be removed during another portion of the process, including, but not limited to the separation zone or the downstream hydrocarbon conversion zone. This may be accomplished with or without modification to these particular zones, reactors, or processes.
- the contaminant removal zone is often positioned downstream of the hydrocarbon conversion reactor, it should be understood that the contaminant removal zone in accordance herewith may be positioned upstream of the separation zone, between the separation zone and the hydrocarbon conversion zone, or downstream of the hydrocarbon conversion zone or along other streams within the process stream, such as, for example, a carrier fluid stream, a fuel stream, an oxygen source stream, or any streams used in the systems and the processes described herein.
- the contaminant concentration is controlled by removing at least a portion of the contaminant from the coal tar stream 30 .
- the term removing may refer to actual removal, for example by adsorption, absorption, or membrane separation, or it may refer to conversion of the contaminant to a more tolerable compound, or both.
- Typical adsorbents include, but are not limited to, a noble metal deposited on a support selected from the group consisting of molecular sieves, alumina, activated carbons, and silica gel; silver impregnated zeolite selected from the group consisting of faujasites (13X, CaX, NaY, CaY, and ZnX), chabazites, clinoptilolites and LTA (3A, 4A, 5A) zeolites; sulfur or a metal sulfide on an activated carbon support or an activated alumina support; or a metal sulfide, metal oxide, or metal carbonate on a support, the metal is selected from the group consisting of copper, silver, gold, antimony, lead, and manganese, and the support selected from the group consisting of activated alumina, clay, or activated
- the viscosity of the coal tar stream can be reduced before it is contacted with the extraction agent or adsorbent using any suitable method, if desired.
- the viscosity can be reduced before or after the optional contaminant removal zone, for example.
- Suitable methods for reducing the viscosity of the coal tar stream include, but are not limited to, mixing the coal tar stream with a solvent (not shown).
- Coal tar comprises a complex mixture of heterocyclic aromatic compounds and their derivatives with a wide range of boiling points.
- the number of fractions and the components in the various fractions can be varied as is well known in the art.
- a typical separation process involves separating the coal tar into four to six streams. For example, there can be a fraction comprising NH 3 , CO, and light hydrocarbons, a light oil fraction with boiling points between 0° C. and 180° C., a middle oil fraction with boiling points between 180° C. to 230° C., a heavy oil fraction with boiling points between 230 to 270° C., an anthracene oil fraction with boiling points between 270° C. to 350° C., and pitch.
- the light oil fraction contains compounds such as benzenes, toluenes, xylenes, naphtha, coumarone-indene, dicyclopentadiene, pyridine, and picolines.
- the middle oil fraction contains compounds such as phenols, cresols and cresylic acids, xylenols, naphthalene, high boiling tar acids, and high boiling tar bases.
- the heavy oil fraction contains benzene absorbing oil and creosotes.
- the anthracene oil fraction contains anthracene.
- Pitch is the residue of the coal tar distillation containing primarily aromatic hydrocarbons and heterocyclic compounds.
- the coal tar feed 40 is separated into gas fraction 50 containing gases such as NH 3 and CO as well as light hydrocarbons, such as ethane, hydrocarbon fractions 55 , 60 , and 65 having different boiling point ranges, and pitch fraction 70 .
- Suitable separation processes include, but are not limited to fractionation, solvent extraction, and adsorption.
- One or more of the fractions 50 , 55 , 60 , 65 , 70 can be further processed, as desired.
- fraction 60 is sent to treatment zone 61 for extraction or adsorption.
- an extraction agent stream 62 is introduced into the treatment zone 61 and contacts the decontaminated coal tar stream.
- the extraction agent stream 62 can be between 1 and 99 wt % of the mixture of extraction agent stream and coal tar stream in the treatment zone.
- the extraction can be performed at a temperature between 0° C. and 250° C. When the extraction agent contains a supercritical component, the temperature is that required for the supercritical conditions of the chosen supercritical component.
- the extraction agent and the product are separated.
- the extraction agent can be recycled, if desired.
- At least one contaminant 63 is removed from the fraction 60 .
- the contaminant(s) can then be recovered and sent for additional treatment, if needed (not shown).
- the extraction agent can be one or more of amphiphilic block copolymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, cyclodextrins, functionalized cyclodextrins, and cyclodextrin-functionalized polymers.
- Cyclodextrins are cyclic oligosaccharides. They have a characteristic toroidal shape that form well defined cavities. The cavities are typically about 8 ⁇ deep and have a diameter of about 5 to 10 nm depending on the number of the glucose units. The outside of the cavity is hydrophilic because of the presence of hydroxyl groups, while the inner cavity is hydrophobic because of presence of carbon and hydrogen atoms. CDs can accommodate guest molecules in the cavity. Typically, the less polar part of the guest molecule is in the cavity, and the more polar part is outside. The hydroxyls on the outside of the CDs can be functionalized, and functionalized CDs can be polymerized. Ionic liquids can be used to functionalize CDs. CDs can be functionalized to modify their properties and/or to introduce groups with specific activity. Functionalization can involve one or more hydroxyl groups.
- CDs, functionalized CDs, and CD-functionalized polymers are described in Ondo et al., Interaction of Ionic Liquids Ions with Natural Cyclodextrins, J. Phys. Chem. B, 2011, 115, 10285-10297; He et al., Interaction of Ionic Liquids Ions and ⁇ -Cyclodextrin, J. Phys. Chem.
- Inclusion complexes of polymethyl methacrylate and polycyclic aromatic hydrocarbons can also be used as extraction agents.
- Syndiotactic polymethyl methacrylate can form a helical cavity in which polycyclic aromatic hydrocarbons are contained. Formation of inclusion complexes is described in Kawauchi et al., Formation of the Inclusion Complex of Helical Syndiotactic Poly(methyl methacrylate) and Polycyclic Aromatic Hydrocarbons, Macromolecules, 2011, 44, 3452-3457, which is incorporated herein by reference.
- Amphiphilic block copolymers have alternating hydrophilic polymer blocks and hydrophobic polymer blocks.
- the amphiphilic block copolymer comprises at least two blocks selected from polyethylene oxide (EO) blocks, polypropylene oxide (PO) blocks, butylene oxide (BO) blocks, silicone (SC) blocks, urethane (UO) blocks, polyurethane ionomer (PI) blocks, acrylate ionomer (AI) blocks, polymethylacryate (MA) blocks, polyacrylic acid (AA) blocks, and polyvinylidene chloride (VC) blocks.
- EO polyethylene oxide
- PO polypropylene oxide
- BO butylene oxide
- SC silicone
- UO urethane
- PI polyurethane ionomer
- AI acrylate ionomer
- MA polymethylacryate
- MA polyacrylic acid
- VC polyvinylidene chloride
- amphiphilic block copolymers include, but are not limited to, EO-PO, EO-PO-EO, PO-EO-PO, EO-BO, PI-EO, AI-EO, SI-EO, and the like. There are typically two or three different blocks in the block copolymers.
- Amphiphilic block copolymers are described in Tungittiplakorn et al., “Engineered Polymeric Nanoparticles for Soil Remediation,” Environ. Sci. Technol. 2004, 38, 1605-1610; Tungittiplakorn et al., “Engineered Polymeric Nanoparticles for Bioremediation of Hydrophobic Contaminants,” Environ. Sci. Technol.
- the CDs, functionalized CDs, CD-functionalized polymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, and amphiphilic block copolymer can optionally be dissolved in ionic liquids, supercritical fluids, or both. Alternatively, they can be used without an ionic liquid, or supercritical fluid, if desired.
- Ionic liquids are non-aqueous, organic salts composed of ions where the positive ion is charge balanced with a negative ion. These materials have low melting points, often below 100° C., undetectable vapor pressure, and good chemical and thermal stability.
- the cationic charge of the salt is localized over hetero atoms, such as nitrogen, phosphorous, sulfur, arsenic, boron, antimony, and aluminum, and the anions may be any inorganic, organic, or organometallic species.
- Suitable ionic liquids include, but are not limited to, imidazolium-based ionic liquids, pyrrolidinium-based ionic liquids, pyridinium-based ionic liquids, sulphonium-based ionic liquids, phosphonium-based ionic liquids, and ammonium-based ionic liquids, and combinations thereof
- Supercritical fluids are substances at a temperature and pressure above the critical point, where distinct liquid and gas phases do not exist. They have properties of both liquids and vapors. Suitable supercritical fluids include, but are not limited to, supercritical carbon dioxide, supercritical ammonia, supercritical ethane, supercritical propane, supercritical butane, and supercritical water, and combinations thereof. In some embodiments, the gas fraction from the separation zone can be used as the source of the carbon dioxide or ammonia for the supercritical carbon dioxide or supercritical ammonia.
- the fraction 60 is sent to treatment zone 61 and contacted with an adsorbent.
- the adsorption is typically performed at temperatures between about 0° C. and about 150° C.
- a desorbent is introduced into the bed, and the contaminant is then recovered from the desorbent/contaminant mixture.
- the bed can be heated to remove the adsorbed contaminant.
- the coal tar stream is piped to another adsorbent bed during desorption of the first bed.
- the adsorbent comprises exfoliated graphite oxide, thermally exfoliated graphite oxide or intercalated graphite compounds.
- Exfoliated graphite oxide, thermally exfoliated graphite oxide, and intercalated graphite compounds are described in Hristea et al., Characterization of Exfoliated Graphite for Heavy Oil Sorption, J. Thermal Anal. And calorimetry, Vol.
- the contaminants from the extraction or adsorption process include, but are not limited to, nitrogen heterocyclic aromatics, oxygen heterocyclic aromatics, and sulfur heterocyclic aromatics and combinations thereof.
- At least two contaminants are removed from the fraction 60 .
- the first product can be removed using a first extraction agent or adsorbent, and then the second product can removed using a second extraction agent or adsorbent.
- the contaminants are removed from fraction 60 .
- the treatment zone 61 can be located in various positions along the process depending on the impact of the particular contaminant on the product or process, as discussed above with respect to the optional contaminant removal zone 35 .
- the treatment zone 61 could be located before, after, or in place of, the optional contaminant removal zone 35 , before or after the separation zone 45 , or before or after the hydrocarbon conversion zone 75 , as well as in other suitable locations.
- a portion of the coal tar stream is treated (fraction 60 as illustrated).
- all or a portion of the coal tar stream 30 could be treated.
- the treated fraction 64 can be sent to one or more hydrocarbon conversion zones.
- the treated fraction can be sent to hydrocarbon conversion zone 75 for hydrocracking, for example, to produce product 85 .
- Suitable hydrocarbon conversion zones include, but are not limited to, hydrotreating zones, hydrocracking zones fluid catalytic cracking zones, alkylation zones, transalkylation zones, oxidation zones and hydrogenation zones.
- Hydrotreating is a process in which hydrogen gas is contacted with a hydrocarbon stream in the presence of suitable catalysts which are primarily active for the removal of heteroatoms, such as sulfur, nitrogen, oxygen, and metals from the hydrocarbon feedstock.
- suitable catalysts which are primarily active for the removal of heteroatoms, such as sulfur, nitrogen, oxygen, and metals from the hydrocarbon feedstock.
- hydrocarbons with double and triple bonds may be saturated.
- Aromatics may also be saturated.
- Typical hydrotreating reaction conditions include a temperature of about 290° C. (550° F.) to about 455° C.
- Typical hydrotreating catalysts include at least one Group VIII metal, preferably iron, cobalt and nickel, and at least one Group VI metal, preferably molybdenum and tungsten, on a high surface area support material, preferably alumina
- Other typical hydrotreating catalysts include zeolitic catalysts, as well as noble metal catalysts where the noble metal is selected from palladium and platinum.
- Hydrocracking is a process in which hydrocarbons crack in the presence of hydrogen to lower molecular weight hydrocarbons.
- Typical hydrocracking conditions may include a temperature of about 290° C. (550° F.) to about 468° C. (875° F.), a pressure of about 3.5 MPa (500 psig) to about 20.7 MPa (3000 psig), a liquid hourly space velocity (LHSV) of about 1.0 to less than about 2.5 hr ⁇ 1 , and a hydrogen rate of about 421 to about 2,527 Nm 3 /m 3 oil (2,500-15,000 scf/bbl).
- Typical hydrocracking catalysts include amorphous silica-alumina bases or low-level zeolite bases combined with one or more Group VIII or Group VIB metal hydrogenating components, or a crystalline zeolite cracking base upon which is deposited a Group VIII metal hydrogenating component. Additional hydrogenating components may be selected from Group VIB for incorporation with the zeolite base.
- Fluid catalytic cracking is a catalytic hydrocarbon conversion process accomplished by contacting heavier hydrocarbons in a fluidized reaction zone with a catalytic particulate material.
- the reaction in catalytic cracking is carried out in the absence of substantial added hydrogen or the consumption of hydrogen.
- the process typically employs a powdered catalyst having the particles suspended in a rising flow of feed hydrocarbons to form a fluidized bed.
- cracking takes place in a riser, which is a vertical or upward sloped pipe.
- a pre-heated feed is sprayed into the base of the riser via feed nozzles where it contacts hot fluidized catalyst and is vaporized on contact with the catalyst, and the cracking occurs converting the high molecular weight oil into lighter components including liquefied petroleum gas (LPG), gasoline, and a distillate.
- LPG liquefied petroleum gas
- the catalyst-feed mixture flows upward through the riser for a short period (a few seconds), and then the mixture is separated in cyclones.
- the hydrocarbons are directed to a fractionator for separation into LPG, gasoline, diesel, kerosene, jet fuel, and other possible fractions.
- the cracking catalyst While going through the riser, the cracking catalyst is deactivated because the process is accompanied by formation of coke which deposits on the catalyst particles.
- Contaminated catalyst is separated from the cracked hydrocarbon vapors and is further treated with steam to remove hydrocarbon remaining in the pores of the catalyst.
- the catalyst is then directed into a regenerator where the coke is burned off the surface of the catalyst particles, thus restoring the catalyst's activity and providing the necessary heat for the next reaction cycle.
- the process of cracking is endothermic.
- the regenerated catalyst is then used in the new cycle.
- Typical FCC conditions include a temperature of about 400° C. to about 800° C., a pressure of about 0 to about 688 kPa g (about 0 to 100 psig), and contact times of about 0.1 seconds to about 1 hour. The conditions are determined based on the hydrocarbon feedstock being cracked, and the cracked products desired.
- Zeolite-based catalysts are commonly used in FCC reactors, as are composite catalysts which contain zeolites, silica-aluminas, alumina, and other binders.
- Transalkylation is a chemical reaction resulting in transfer of an alkyl group from one organic compound to another. Catalysts, particularly zeolite catalysts, are often used to effect the reaction. If desired, the transalkylation catalyst may be metal stabilized using a noble metal or base metal, and may contain suitable binder or matrix material such as inorganic oxides and other suitable materials.
- a transalkylation process a polyalkylaromatic hydrocarbon feed and an aromatic hydrocarbon feed are provided to a transalkylation reaction zone. The feed is usually heated to reaction temperature and then passed through a reaction zone, which may comprise one or more individual reactors. Passage of the combined feed through the reaction zone produces an effluent stream comprising unconverted feed and product monoalkylated hydrocarbons.
- This effluent is normally cooled and passed to a stripping column in which substantially all C5 and lighter hydrocarbons present in the effluent are concentrated into an overhead stream and removed from the process.
- An aromatics-rich stream is recovered as net stripper bottoms, which is referred to as the transalkylation effluent.
- the transalkylation reaction can be effected in contact with a catalytic composite in any conventional or otherwise convenient manner and may comprise a batch or continuous type of operation, with a continuous operation being preferred.
- the transalkylation catalyst is usefully disposed as a fixed bed in a reaction zone of a vertical tubular reactor, with the alkylaromatic feed stock charged through the bed in an upflow or downflow manner.
- the transalkylation zone normally operates at conditions including a temperature in the range of about 130° C. to about 540° C.
- the transalkylation zone is typically operated at moderately elevated pressures broadly ranging from about 100 kPa to about 10 MPa absolute.
- the transalkylation reaction can be effected over a wide range of space velocities. That is, volume of charge per volume of catalyst per hour, weight hourly space velocity (WHSV), is generally in the range of from about 0.1 to about 30 hr ⁇ 1 .
- the catalyst is typically selected to have relatively high stability at a high activity level.
- Alkylation is typically used to combine light olefins, for example mixtures of alkenes such as propylene and butylene, with isobutane to produce a relatively high-octane branched-chain paraffinic hydrocarbon fuel, including isoheptane and isooctane.
- an alkylation reaction can be performed using an aromatic compound such as benzene in place of the isobutane.
- the product resulting from the alkylation reaction is an alkylbenzene (e.g. toluene, xylenes, ethylbenzene, etc.).
- the reactants are mixed in the presence of a strong acid catalyst, such as sulfuric acid or hydrofluoric acid.
- a strong acid catalyst such as sulfuric acid or hydrofluoric acid.
- the alkylation reaction is carried out at mild temperatures, and is typically a two-phase reaction. Because the reaction is exothermic, cooling is needed. Depending on the catalyst used, normal refinery cooling water provides sufficient cooling. Alternatively, a chilled cooling medium can be provided to cool the reaction.
- the catalyst protonates the alkenes to produce reactive carbocations which alkylate the isobutane reactant, thus forming branched chain paraffins from isobutane.
- Aromatic alkylation is generally now conducted with solid acid catalysts including zeolites or amorphous silica-aluminas.
- the alkylation reaction zone is maintained at a pressure sufficient to maintain the reactants in liquid phase.
- a general range of operating pressures is from about 200 to about 7100 kPa absolute.
- the temperature range covered by this set of conditions is from about ⁇ 20° C. to about 200° C.
- the volumetric ratio of hydrofluoric acid to the total amount of hydrocarbons entering the reactor should be maintained within the broad range of from about 0.2:1 to about 10:1, preferably from about 0.5:1 to about 2:1
- syngas 105 is a mixture of carbon monoxide and hydrogen.
- the syngas 105 can be further processed using the Fischer-Tropsch reaction to produce gasoline or using the water-gas shift reaction to produce more hydrogen.
- Oxidation involves the oxidation of hydrocarbons to oxygen-containing compounds, such as aldehydes.
- the hydrocarbons include alkanes, alkenes, typically with carbon numbers from 2 to 15, and alkyl aromatics, Linear, branched, and cyclic alkanes and alkenes can be used.
- Oxygenates that are not fully oxidized to ketones or carboxylic acids can also be subjected to oxidation processes, as well as sulfur compounds that contain —S—H moieties, thiophene rings, and sulfone groups.
- the process is carried out by placing an oxidation catalyst in a reaction zone and contacting the feed stream which contains the desired hydrocarbons with the catalyst in the presence of oxygen.
- the type of reactor which can be used is any type well known in the art such as fixed-bed, moving-bed, multi-tube, CS IR, fluidized bed, etc.
- the feed stream can be flowed over the catalyst bed either up-flow or down-flow in the liquid, vapor, or mixed phase. In the case of a fluidized-bed, the feed stream can be flowed co-current or counter-current. In a CSTR the feed stream can be continuously added or added batch-wise.
- the feed stream contains the desired oxidizable species along with oxygen. Oxygen can be introduced either as pure oxygen or as air, or as liquid phase oxidants including hydrogen peroxide, organic peroxides, or peroxy-acids.
- the molar ratio of oxygen (O 2 ) to substrate to be oxidized can range from about 5:1 to about 1:10.
- the feed stream can also contain a diluent gas selected form nitrogen, neon, argon, helium, carbon dioxide, steam or mixtures thereof As stated, the oxygen can be added as air which could also provide a diluent.
- the molar ratio of diluent gas to oxygen ranges from greater than zero to about 10:1.
- the catalyst and feed stream are reacted at oxidation conditions which include a temperature of about 25° C. to about 600° C., a pressure of about 101 kPa to about 5,066 kPa and a space velocity of about 100 to about 100,000 hr ⁇ 1 .
- Hydrogenation involves the addition of hydrogen to hydrogenatable hydrocarbon compounds.
- hydrogen can be provided in a hydrogen-containing compound with ready available hydrogen, such as tetralin, alcohols, hydrogenated naphthalenes, and others via a transfer hydrogenation process with or without a catalyst.
- the hydrogenatable hydrocarbon compounds are introduced into a hydrogenation zone and contacted with a hydrogen-rich gaseous phase and a hydrogenation catalyst in order to hydrogenate at least a portion of the hydrogenatable hydrocarbon compounds.
- the catalytic hydrogenation zone may contain a fixed, ebulated or fluidized catalyst bed. Alternatively the hydrogenation process can be carried out in the liquid phase in a CSTR.
- This reaction zone is typically at a pressure from about 689 k Pa gauge (100 psig) to about 13790 k Pa gauge (2000 psig) with a maximum catalyst bed temperature in the range of about 177° C. (350° F.) to about 454° C. (850° F.).
- the liquid hourly space velocity is typically in the range from about 0.2 hr ⁇ 1 to about 10 hr ⁇ 1 and hydrogen circulation rates from about 200 standard cubic feet per barrel (SCFB) (35.6 m 3 /m 3 ) to about 10,000 SCFB (1778 m 3 /m 3 ).
Abstract
A process for removing at least one contaminant from coal tar is described. The process involves extraction with an extraction agent or adsorption with an adsorbent. The extraction agent includes at least one of amphiphilic block copolymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, cyclodextrins, functionalized cyclodextrins, and cyclodextrin-functionalized polymers, and the adsorbent includes exfoliated graphite oxide, thermally exfoliated graphite oxide or intercalated graphite compounds.
Description
- This application claims the benefit of Provisional Application Ser. No. 61/905,895 filed Nov. 19, 2013, entitled Process for Removing a Contaminant from Coal Tar.
- Many different types of chemicals are produced from the processing of petroleum. However, petroleum is becoming more expensive because of increased demand in recent decades.
- Therefore, attempts have been made to provide alternative sources for the starting materials for manufacturing chemicals. Attention is now being focused on producing liquid hydrocarbons from solid carbonaceous materials, such as coal, which is available in large quantities in countries such as the United States and China.
- Pyrolysis of coal produces coke and coal tar. The coke-making or “coking” process consists of heating the material in closed vessels in the absence of oxygen to very high temperatures. Coke is a porous but hard residue that is mostly carbon and inorganic ash, which is used in making steel.
- Coal tar is the volatile material that is driven off during heating, and it comprises a mixture of a number of hydrocarbon compounds. It can be separated to yield a variety of organic compounds, such as benzene, toluene, xylene, naphthalene, anthracene, and phenanthrene. These organic compounds can be used to make numerous products, for example, dyes, drugs, explosives, flavorings, perfumes, preservatives, synthetic resins, and paints and stains but may also be processed into fuels and petrochemical intermediates. The residual pitch left from the separation is used for paving, roofing, waterproofing, and insulation.
- Coal tar has a number of contaminants that need to be removed, such as nitrogen, oxygen, or sulfur-containing compounds.
- There is a need for additional processes for removing contaminants from coal tar.
- One aspect of the invention is a process for removing at least one product from coal tar. In one embodiment, the process includes providing at least a portion of a coal tar stream; removing at least one contaminant from the at least the portion of the coal tar stream by extraction with an extraction agent or adsorption with an adsorbent to form a treated coal tar stream having a reduced level of the at least one contaminant, the extraction agent comprising at least one of amphiphilic block copolymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, cyclodextrins, functionalized cyclodextrins, and cyclodextrin-functionalized polymers, the adsorbent comprising exfoliated graphite oxide, thermally exfoliated graphite oxide or intercalated graphite compounds, and the at least one contaminant comprising nitrogen heterocyclic aromatics, oxygen heterocyclic aromatics, and sulfur heterocyclic aromatics; and separating the at least the portion of the coal tar stream into at least two fractions.
- The FIGURE is an illustration of one embodiment of the process of the present invention.
- The FIGURE shows one embodiment of a
coal conversion process 5. Thecoal feed 10 can be sent to thepyrolysis zone 15, thegasification zone 20, or thecoal feed 10 can be split into two parts and sent to both. - In the
pyrolysis zone 15, the coal is heated at high temperature, e.g., up to about 2,000° C. (3600° F.), in the absence of oxygen to drive off the volatile components. Coking produces acoke stream 25 and acoal tar stream 30. Thecoke stream 25 can be used in other processes, such as the manufacture of steel. - The
coal tar stream 30 which comprises the volatile components from the coking process can be sent to an optionalcontaminant removal zone 35, if desired. - The
contaminant removal zone 35 for removing one or more contaminants from the coal tar stream or another process stream may be located at various positions along the process depending on the impact of the particular contaminant on the product or process and the reason for the contaminant's removal, as described further below. For example, thecontaminant removal zone 35 can be positioned upstream of theseparation zone 45, as shown in the FIGURE. Some contaminants have been identified to interfere with a downstream processing step or hydrocarbon conversion process, in which case thecontaminant removal zone 35 may be positioned upstream of theseparation zone 45 or between theseparation zone 45 and the particular downstream processing step at issue. Still other contaminants have been identified that should be removed to meet particular product specifications. Where it is desired to remove multiple contaminants from the hydrocarbon or process stream, various contaminant removal zones may be positioned at different locations along the process. In still other approaches, a contaminant removal zone may overlap or be integrated with another process within the system, in which case the contaminant may be removed during another portion of the process, including, but not limited to the separation zone or the downstream hydrocarbon conversion zone. This may be accomplished with or without modification to these particular zones, reactors, or processes. While the contaminant removal zone is often positioned downstream of the hydrocarbon conversion reactor, it should be understood that the contaminant removal zone in accordance herewith may be positioned upstream of the separation zone, between the separation zone and the hydrocarbon conversion zone, or downstream of the hydrocarbon conversion zone or along other streams within the process stream, such as, for example, a carrier fluid stream, a fuel stream, an oxygen source stream, or any streams used in the systems and the processes described herein. The contaminant concentration is controlled by removing at least a portion of the contaminant from thecoal tar stream 30. As used herein, the term removing may refer to actual removal, for example by adsorption, absorption, or membrane separation, or it may refer to conversion of the contaminant to a more tolerable compound, or both. - Conventional contaminant removal methods can be used for the optional
contaminant removal zone 35, including, but not limited to, adsorption and oxidation. Typical adsorbents include, but are not limited to, a noble metal deposited on a support selected from the group consisting of molecular sieves, alumina, activated carbons, and silica gel; silver impregnated zeolite selected from the group consisting of faujasites (13X, CaX, NaY, CaY, and ZnX), chabazites, clinoptilolites and LTA (3A, 4A, 5A) zeolites; sulfur or a metal sulfide on an activated carbon support or an activated alumina support; or a metal sulfide, metal oxide, or metal carbonate on a support, the metal is selected from the group consisting of copper, silver, gold, antimony, lead, and manganese, and the support selected from the group consisting of activated alumina, clay, or activated carbon. - The viscosity of the coal tar stream can be reduced before it is contacted with the extraction agent or adsorbent using any suitable method, if desired. The viscosity can be reduced before or after the optional contaminant removal zone, for example. Suitable methods for reducing the viscosity of the coal tar stream include, but are not limited to, mixing the coal tar stream with a solvent (not shown).
- The decontaminated
coal tar stream 40 from thecontaminant removal zone 35 is sent to aseparation zone 45 where it is separated into two or more fractions. Coal tar comprises a complex mixture of heterocyclic aromatic compounds and their derivatives with a wide range of boiling points. The number of fractions and the components in the various fractions can be varied as is well known in the art. A typical separation process involves separating the coal tar into four to six streams. For example, there can be a fraction comprising NH3, CO, and light hydrocarbons, a light oil fraction with boiling points between 0° C. and 180° C., a middle oil fraction with boiling points between 180° C. to 230° C., a heavy oil fraction with boiling points between 230 to 270° C., an anthracene oil fraction with boiling points between 270° C. to 350° C., and pitch. - The light oil fraction contains compounds such as benzenes, toluenes, xylenes, naphtha, coumarone-indene, dicyclopentadiene, pyridine, and picolines. The middle oil fraction contains compounds such as phenols, cresols and cresylic acids, xylenols, naphthalene, high boiling tar acids, and high boiling tar bases. The heavy oil fraction contains benzene absorbing oil and creosotes. The anthracene oil fraction contains anthracene. Pitch is the residue of the coal tar distillation containing primarily aromatic hydrocarbons and heterocyclic compounds.
- As illustrated, the
coal tar feed 40 is separated intogas fraction 50 containing gases such as NH3 and CO as well as light hydrocarbons, such as ethane,hydrocarbon fractions pitch fraction 70. - Suitable separation processes include, but are not limited to fractionation, solvent extraction, and adsorption.
- One or more of the
fractions - As illustrated,
fraction 60 is sent totreatment zone 61 for extraction or adsorption. - In an extraction process, an
extraction agent stream 62 is introduced into thetreatment zone 61 and contacts the decontaminated coal tar stream. Theextraction agent stream 62 can be between 1 and 99 wt % of the mixture of extraction agent stream and coal tar stream in the treatment zone. The extraction can be performed at a temperature between 0° C. and 250° C. When the extraction agent contains a supercritical component, the temperature is that required for the supercritical conditions of the chosen supercritical component. - The extraction agent and the product are separated. The extraction agent can be recycled, if desired. At least one contaminant 63 is removed from the
fraction 60. The contaminant(s) can then be recovered and sent for additional treatment, if needed (not shown). - The extraction agent can be one or more of amphiphilic block copolymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, cyclodextrins, functionalized cyclodextrins, and cyclodextrin-functionalized polymers.
- Cyclodextrins (CDs) are cyclic oligosaccharides. They have a characteristic toroidal shape that form well defined cavities. The cavities are typically about 8 Å deep and have a diameter of about 5 to 10 nm depending on the number of the glucose units. The outside of the cavity is hydrophilic because of the presence of hydroxyl groups, while the inner cavity is hydrophobic because of presence of carbon and hydrogen atoms. CDs can accommodate guest molecules in the cavity. Typically, the less polar part of the guest molecule is in the cavity, and the more polar part is outside. The hydroxyls on the outside of the CDs can be functionalized, and functionalized CDs can be polymerized. Ionic liquids can be used to functionalize CDs. CDs can be functionalized to modify their properties and/or to introduce groups with specific activity. Functionalization can involve one or more hydroxyl groups.
- CDs, functionalized CDs, and CD-functionalized polymers are described in Ondo et al., Interaction of Ionic Liquids Ions with Natural Cyclodextrins, J. Phys. Chem. B, 2011, 115, 10285-10297; He et al., Interaction of Ionic Liquids Ions and β-Cyclodextrin, J. Phys. Chem. B, 2009, 113, 231-238; Mahlambi et al., “Polymerization of Cyclodextrin-Ionic Liquid Complexes for the Removal of Organic and Inorganic Contaminants from Water,” InTech 2011, 115-150, www.intechopen.com; Rogalski et al., Physico-Chemical Properties and Phase Behavior of the Ionic Liquid-β-Cyclodextrin Complexes, Int. J. Mol. Sci. 2013, 14, 16638-16655; Zheng et al., The Enhanced Dissolution of β-Cyclodextrin in Some Hydrophilic Ionic Liquids, J. Phys. Chem. A, 2010, 114, 3926-3931; Uemasu, Effect of Methanol-Water Mixture Solvent on Concentration of Indole in Coal Tar Using α-Cyclodextrin as Complexing Agent, Sekiyu Gakkaishi, 34, (4), 371-374 (1991); each of which is incorporated herein by reference.
- Inclusion complexes of polymethyl methacrylate and polycyclic aromatic hydrocarbons can also be used as extraction agents. Syndiotactic polymethyl methacrylate can form a helical cavity in which polycyclic aromatic hydrocarbons are contained. Formation of inclusion complexes is described in Kawauchi et al., Formation of the Inclusion Complex of Helical Syndiotactic Poly(methyl methacrylate) and Polycyclic Aromatic Hydrocarbons, Macromolecules, 2011, 44, 3452-3457, which is incorporated herein by reference.
- Amphiphilic block copolymers have alternating hydrophilic polymer blocks and hydrophobic polymer blocks. The amphiphilic block copolymer comprises at least two blocks selected from polyethylene oxide (EO) blocks, polypropylene oxide (PO) blocks, butylene oxide (BO) blocks, silicone (SC) blocks, urethane (UO) blocks, polyurethane ionomer (PI) blocks, acrylate ionomer (AI) blocks, polymethylacryate (MA) blocks, polyacrylic acid (AA) blocks, and polyvinylidene chloride (VC) blocks. Examples of suitable amphiphilic block copolymers include, but are not limited to, EO-PO, EO-PO-EO, PO-EO-PO, EO-BO, PI-EO, AI-EO, SI-EO, and the like. There are typically two or three different blocks in the block copolymers.
- Amphiphilic block copolymers are described in Tungittiplakorn et al., “Engineered Polymeric Nanoparticles for Soil Remediation,” Environ. Sci. Technol. 2004, 38, 1605-1610; Tungittiplakorn et al., “Engineered Polymeric Nanoparticles for Bioremediation of Hydrophobic Contaminants,” Environ. Sci. Technol. 2005, 39, 1354-1358; Qiao et al, “Stabilized Micelles of Amphoteric Polyurethane Formed by Thermoresponsive Micellization in HCl Aqueous Solution,” Langmuir, 2008, 24, 3122-3126; Velasquez et al., Poly(vinylidene chloride)-Based Amphiphilic Block Copolymers, Macromolecules, 2013, 46, 664-673; and U.S. Publication Nos. 2013/0030131, 2008/0045687, each of which is incorporated herein by reference.
- The CDs, functionalized CDs, CD-functionalized polymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, and amphiphilic block copolymer can optionally be dissolved in ionic liquids, supercritical fluids, or both. Alternatively, they can be used without an ionic liquid, or supercritical fluid, if desired.
- Ionic liquids are non-aqueous, organic salts composed of ions where the positive ion is charge balanced with a negative ion. These materials have low melting points, often below 100° C., undetectable vapor pressure, and good chemical and thermal stability. The cationic charge of the salt is localized over hetero atoms, such as nitrogen, phosphorous, sulfur, arsenic, boron, antimony, and aluminum, and the anions may be any inorganic, organic, or organometallic species. Suitable ionic liquids include, but are not limited to, imidazolium-based ionic liquids, pyrrolidinium-based ionic liquids, pyridinium-based ionic liquids, sulphonium-based ionic liquids, phosphonium-based ionic liquids, and ammonium-based ionic liquids, and combinations thereof
- Supercritical fluids are substances at a temperature and pressure above the critical point, where distinct liquid and gas phases do not exist. They have properties of both liquids and vapors. Suitable supercritical fluids include, but are not limited to, supercritical carbon dioxide, supercritical ammonia, supercritical ethane, supercritical propane, supercritical butane, and supercritical water, and combinations thereof. In some embodiments, the gas fraction from the separation zone can be used as the source of the carbon dioxide or ammonia for the supercritical carbon dioxide or supercritical ammonia.
- Alternatively, the
fraction 60 is sent totreatment zone 61 and contacted with an adsorbent. The adsorption is typically performed at temperatures between about 0° C. and about 150° C. In one embodiment, after the adsorbent bed is fully loaded to capacity, a desorbent is introduced into the bed, and the contaminant is then recovered from the desorbent/contaminant mixture. Alternatively, the bed can be heated to remove the adsorbed contaminant. In some embodiments, the coal tar stream is piped to another adsorbent bed during desorption of the first bed. - The adsorbent comprises exfoliated graphite oxide, thermally exfoliated graphite oxide or intercalated graphite compounds. Exfoliated graphite oxide, thermally exfoliated graphite oxide, and intercalated graphite compounds are described in Hristea et al., Characterization of Exfoliated Graphite for Heavy Oil Sorption, J. Thermal Anal. And calorimetry, Vol. 91 (2008) 3, 817-823; Tryba et al., Influence of chemically prepared H2SO4-graphite intercalation compound (GIC) precursor on parameters of exfoliated graphite (EG) for oil sorption from water, Carbon, 41 (2002) 2009-2025; Tryba et al., Exfoliated graphite as a New Sorbent for Removal of Engine Oils from Wastewater, Spill Science and Tech. Bull., Vol. 8, Nos. 5-6, 569-571; Toyoda et al., Heavy oil sorption using exfoliated graphite New application of exfoliated graphite to protect heavy oil pollution, Carbon, 38 (2000) 199-210; and U.S. Pat. No. 7,658,901, each of which is incorporated herein by reference.
- The contaminants from the extraction or adsorption process include, but are not limited to, nitrogen heterocyclic aromatics, oxygen heterocyclic aromatics, and sulfur heterocyclic aromatics and combinations thereof.
- In some embodiments, at least two contaminants are removed from the
fraction 60. The first product can be removed using a first extraction agent or adsorbent, and then the second product can removed using a second extraction agent or adsorbent. - As shown, the contaminants are removed from
fraction 60. As will be understood by those of skill in the art, thetreatment zone 61 can be located in various positions along the process depending on the impact of the particular contaminant on the product or process, as discussed above with respect to the optionalcontaminant removal zone 35. Thetreatment zone 61 could be located before, after, or in place of, the optionalcontaminant removal zone 35, before or after theseparation zone 45, or before or after thehydrocarbon conversion zone 75, as well as in other suitable locations. When thetreatment zone 61 is located after theseparation zone 45 as illustrated, a portion of the coal tar stream is treated (fraction 60 as illustrated). When thetreatment zone 61 is located before theseparation zone 45, all or a portion of thecoal tar stream 30 could be treated. - The treated
fraction 64 can be sent to one or more hydrocarbon conversion zones. For example, the treated fraction can be sent tohydrocarbon conversion zone 75 for hydrocracking, for example, to produceproduct 85. Suitable hydrocarbon conversion zones include, but are not limited to, hydrotreating zones, hydrocracking zones fluid catalytic cracking zones, alkylation zones, transalkylation zones, oxidation zones and hydrogenation zones. - Hydrotreating is a process in which hydrogen gas is contacted with a hydrocarbon stream in the presence of suitable catalysts which are primarily active for the removal of heteroatoms, such as sulfur, nitrogen, oxygen, and metals from the hydrocarbon feedstock. In hydrotreating, hydrocarbons with double and triple bonds may be saturated. Aromatics may also be saturated. Typical hydrotreating reaction conditions include a temperature of about 290° C. (550° F.) to about 455° C. (850° F.), a pressure of about 3.4 MPa (500 psig) to about 27.6 MPa (4000 psig), a liquid hourly space velocity of about 0.5 hr−1 to about 4 hr−1, and a hydrogen rate of about 168 to about 1,011 Nm3/m3 oil (1,000-6,000 scf/bbl). Typical hydrotreating catalysts include at least one Group VIII metal, preferably iron, cobalt and nickel, and at least one Group VI metal, preferably molybdenum and tungsten, on a high surface area support material, preferably alumina Other typical hydrotreating catalysts include zeolitic catalysts, as well as noble metal catalysts where the noble metal is selected from palladium and platinum.
- Hydrocracking is a process in which hydrocarbons crack in the presence of hydrogen to lower molecular weight hydrocarbons. Typical hydrocracking conditions may include a temperature of about 290° C. (550° F.) to about 468° C. (875° F.), a pressure of about 3.5 MPa (500 psig) to about 20.7 MPa (3000 psig), a liquid hourly space velocity (LHSV) of about 1.0 to less than about 2.5 hr−1, and a hydrogen rate of about 421 to about 2,527 Nm3/m3 oil (2,500-15,000 scf/bbl). Typical hydrocracking catalysts include amorphous silica-alumina bases or low-level zeolite bases combined with one or more Group VIII or Group VIB metal hydrogenating components, or a crystalline zeolite cracking base upon which is deposited a Group VIII metal hydrogenating component. Additional hydrogenating components may be selected from Group VIB for incorporation with the zeolite base.
- Fluid catalytic cracking (FCC) is a catalytic hydrocarbon conversion process accomplished by contacting heavier hydrocarbons in a fluidized reaction zone with a catalytic particulate material. The reaction in catalytic cracking is carried out in the absence of substantial added hydrogen or the consumption of hydrogen. The process typically employs a powdered catalyst having the particles suspended in a rising flow of feed hydrocarbons to form a fluidized bed. In representative processes, cracking takes place in a riser, which is a vertical or upward sloped pipe. Typically, a pre-heated feed is sprayed into the base of the riser via feed nozzles where it contacts hot fluidized catalyst and is vaporized on contact with the catalyst, and the cracking occurs converting the high molecular weight oil into lighter components including liquefied petroleum gas (LPG), gasoline, and a distillate. The catalyst-feed mixture flows upward through the riser for a short period (a few seconds), and then the mixture is separated in cyclones. The hydrocarbons are directed to a fractionator for separation into LPG, gasoline, diesel, kerosene, jet fuel, and other possible fractions. While going through the riser, the cracking catalyst is deactivated because the process is accompanied by formation of coke which deposits on the catalyst particles. Contaminated catalyst is separated from the cracked hydrocarbon vapors and is further treated with steam to remove hydrocarbon remaining in the pores of the catalyst. The catalyst is then directed into a regenerator where the coke is burned off the surface of the catalyst particles, thus restoring the catalyst's activity and providing the necessary heat for the next reaction cycle. The process of cracking is endothermic. The regenerated catalyst is then used in the new cycle. Typical FCC conditions include a temperature of about 400° C. to about 800° C., a pressure of about 0 to about 688 kPa g (about 0 to 100 psig), and contact times of about 0.1 seconds to about 1 hour. The conditions are determined based on the hydrocarbon feedstock being cracked, and the cracked products desired. Zeolite-based catalysts are commonly used in FCC reactors, as are composite catalysts which contain zeolites, silica-aluminas, alumina, and other binders.
- Transalkylation is a chemical reaction resulting in transfer of an alkyl group from one organic compound to another. Catalysts, particularly zeolite catalysts, are often used to effect the reaction. If desired, the transalkylation catalyst may be metal stabilized using a noble metal or base metal, and may contain suitable binder or matrix material such as inorganic oxides and other suitable materials. In a transalkylation process, a polyalkylaromatic hydrocarbon feed and an aromatic hydrocarbon feed are provided to a transalkylation reaction zone. The feed is usually heated to reaction temperature and then passed through a reaction zone, which may comprise one or more individual reactors. Passage of the combined feed through the reaction zone produces an effluent stream comprising unconverted feed and product monoalkylated hydrocarbons. This effluent is normally cooled and passed to a stripping column in which substantially all C5 and lighter hydrocarbons present in the effluent are concentrated into an overhead stream and removed from the process. An aromatics-rich stream is recovered as net stripper bottoms, which is referred to as the transalkylation effluent.
- The transalkylation reaction can be effected in contact with a catalytic composite in any conventional or otherwise convenient manner and may comprise a batch or continuous type of operation, with a continuous operation being preferred. The transalkylation catalyst is usefully disposed as a fixed bed in a reaction zone of a vertical tubular reactor, with the alkylaromatic feed stock charged through the bed in an upflow or downflow manner. The transalkylation zone normally operates at conditions including a temperature in the range of about 130° C. to about 540° C. The transalkylation zone is typically operated at moderately elevated pressures broadly ranging from about 100 kPa to about 10 MPa absolute. The transalkylation reaction can be effected over a wide range of space velocities. That is, volume of charge per volume of catalyst per hour, weight hourly space velocity (WHSV), is generally in the range of from about 0.1 to about 30 hr−1. The catalyst is typically selected to have relatively high stability at a high activity level.
- Alkylation is typically used to combine light olefins, for example mixtures of alkenes such as propylene and butylene, with isobutane to produce a relatively high-octane branched-chain paraffinic hydrocarbon fuel, including isoheptane and isooctane. Similarly, an alkylation reaction can be performed using an aromatic compound such as benzene in place of the isobutane. When using benzene, the product resulting from the alkylation reaction is an alkylbenzene (e.g. toluene, xylenes, ethylbenzene, etc.). For isobutane alkylation, typically, the reactants are mixed in the presence of a strong acid catalyst, such as sulfuric acid or hydrofluoric acid. The alkylation reaction is carried out at mild temperatures, and is typically a two-phase reaction. Because the reaction is exothermic, cooling is needed. Depending on the catalyst used, normal refinery cooling water provides sufficient cooling. Alternatively, a chilled cooling medium can be provided to cool the reaction. The catalyst protonates the alkenes to produce reactive carbocations which alkylate the isobutane reactant, thus forming branched chain paraffins from isobutane. Aromatic alkylation is generally now conducted with solid acid catalysts including zeolites or amorphous silica-aluminas.
- The alkylation reaction zone is maintained at a pressure sufficient to maintain the reactants in liquid phase. For a hydrofluoric acid catalyst, a general range of operating pressures is from about 200 to about 7100 kPa absolute. The temperature range covered by this set of conditions is from about −20° C. to about 200° C. For at least alkylation of aromatic compounds, the volumetric ratio of hydrofluoric acid to the total amount of hydrocarbons entering the reactor should be maintained within the broad range of from about 0.2:1 to about 10:1, preferably from about 0.5:1 to about 2:1
- In some processes, all or a portion of the
coal feed 10 is mixed withoxygen 95 andsteam 100 and reacted under heat and pressure in thegasification zone 20 to formsyngas 105, which is a mixture of carbon monoxide and hydrogen. Thesyngas 105 can be further processed using the Fischer-Tropsch reaction to produce gasoline or using the water-gas shift reaction to produce more hydrogen. - Oxidation involves the oxidation of hydrocarbons to oxygen-containing compounds, such as aldehydes. The hydrocarbons include alkanes, alkenes, typically with carbon numbers from 2 to 15, and alkyl aromatics, Linear, branched, and cyclic alkanes and alkenes can be used. Oxygenates that are not fully oxidized to ketones or carboxylic acids can also be subjected to oxidation processes, as well as sulfur compounds that contain —S—H moieties, thiophene rings, and sulfone groups. The process is carried out by placing an oxidation catalyst in a reaction zone and contacting the feed stream which contains the desired hydrocarbons with the catalyst in the presence of oxygen. The type of reactor which can be used is any type well known in the art such as fixed-bed, moving-bed, multi-tube, CS IR, fluidized bed, etc. The feed stream can be flowed over the catalyst bed either up-flow or down-flow in the liquid, vapor, or mixed phase. In the case of a fluidized-bed, the feed stream can be flowed co-current or counter-current. In a CSTR the feed stream can be continuously added or added batch-wise. The feed stream contains the desired oxidizable species along with oxygen. Oxygen can be introduced either as pure oxygen or as air, or as liquid phase oxidants including hydrogen peroxide, organic peroxides, or peroxy-acids. The molar ratio of oxygen (O2) to substrate to be oxidized can range from about 5:1 to about 1:10. In addition to oxygen and alkane or alkene, the feed stream can also contain a diluent gas selected form nitrogen, neon, argon, helium, carbon dioxide, steam or mixtures thereof As stated, the oxygen can be added as air which could also provide a diluent. The molar ratio of diluent gas to oxygen ranges from greater than zero to about 10:1. The catalyst and feed stream are reacted at oxidation conditions which include a temperature of about 25° C. to about 600° C., a pressure of about 101 kPa to about 5,066 kPa and a space velocity of about 100 to about 100,000 hr−1.
- Hydrogenation involves the addition of hydrogen to hydrogenatable hydrocarbon compounds. Alternatively hydrogen can be provided in a hydrogen-containing compound with ready available hydrogen, such as tetralin, alcohols, hydrogenated naphthalenes, and others via a transfer hydrogenation process with or without a catalyst. The hydrogenatable hydrocarbon compounds are introduced into a hydrogenation zone and contacted with a hydrogen-rich gaseous phase and a hydrogenation catalyst in order to hydrogenate at least a portion of the hydrogenatable hydrocarbon compounds. The catalytic hydrogenation zone may contain a fixed, ebulated or fluidized catalyst bed. Alternatively the hydrogenation process can be carried out in the liquid phase in a CSTR. This reaction zone is typically at a pressure from about 689 k Pa gauge (100 psig) to about 13790 k Pa gauge (2000 psig) with a maximum catalyst bed temperature in the range of about 177° C. (350° F.) to about 454° C. (850° F.). The liquid hourly space velocity is typically in the range from about 0.2 hr−1 to about 10 hr−1 and hydrogen circulation rates from about 200 standard cubic feet per barrel (SCFB) (35.6 m3 /m3) to about 10,000 SCFB (1778 m3/m3).
- While at least one exemplary embodiment has been presented in the foregoing detailed description of the invention, it should be appreciated that a vast number of variations exist. It should also be appreciated that the exemplary embodiment or exemplary embodiments are only examples, and are not intended to limit the scope, applicability, or configuration of the invention in any way. Rather, the foregoing detailed description will provide those skilled in the art with a convenient road map for implementing an exemplary embodiment of the invention. It being understood that various changes may be made in the function and arrangement of elements described in an exemplary embodiment without departing from the scope of the invention as set forth in the appended claims.
Claims (20)
1. A process for removing at least one contaminant from coal tar comprising:
providing at least a portion of a coal tar stream;
removing at least one contaminant from the at least the portion of the coal tar stream by extraction with an extraction agent or adsorption with an adsorbent to form a treated coal tar stream having a reduced level of the at least one contaminant, the extraction agent comprising at least one of amphiphilic block copolymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, cyclodextrins, functionalized cyclodextrins, and cyclodextrin-functionalized polymers, the adsorbent comprising exfoliated graphite oxide, thermally exfoliated graphite oxide or intercalated graphite compounds, and the at least one contaminant comprising nitrogen heterocyclic aromatics, oxygen heterocyclic aromatics, and sulfur heterocyclic aromatics;
separating the at least the portion of the coal tar stream into at least two fractions.
2. The process of claim 1 wherein the extraction agent comprises the amphiphilic block copolymer, and wherein the amphiphilic block copolymer comprises at least two blocks selected from polyethylene oxide blocks, polypropylene oxide blocks, butylene oxide blocks, silicone blocks, urethane blocks, polyurethane ionomer blocks, acrylate ionomer blocks, polymethylacryate blocks, polyacrylic acid blocks, and polyvinylidene chloride blocks.
3. The process of claim 1 wherein the extraction agent further comprises an ionic liquid, or a supercritical fluid, or both.
4. The process of claim 3 wherein the extraction agent further comprises the ionic liquid, and wherein the ionic liquid is selected from imidazolium-based ionic liquid, pyrrolidinium-based ionic liquid, pyridinium-based ionic liquid, sulphonium-based ionic liquids, phosphonium-based ionic liquids, and ammonium-based ionic liquids.
5. The process of claim 3 wherein the extraction agent further comprises the supercritical fluid, and wherein the supercritical fluid comprises supercritical carbon dioxide, supercritical ammonia, supercritical ethane, supercritical propane, supercritical butane, or supercritical water.
6. The process of claim 5 wherein the supercritical fluid is the supercritical ammonia, wherein one of the separated fractions comprises ammonia, and wherein the ammonia in the fraction is processed into the supercritical ammonia.
7. The process of claim 5 wherein the supercritical fluid is the supercritical carbon dioxide, wherein one of the separated fractions comprises carbon dioxide, and wherein the carbon dioxide in the fraction is processed into the supercritical carbon dioxide.
8. The process of claim 1 wherein at least two contaminants are removed, and wherein the first contaminant is removed using a first extraction agent or adsorbent and wherein the second contaminant is removed using a second extraction agent or adsorbent after the removal of the first contaminant and before separating the at least the portion of the coal tar stream into the at least two fractions.
9. The process of claim 1 further comprising removing at least one additional contaminant by adsorption with a second adsorbent, or an oxidation reaction, the at least one additional contaminant comprising arsenic, metal compounds, mercury halides, elemental mercury, inorganic halides, organic halides, and coal tar insolubles, and wherein the second adsorbent comprises a noble metal deposited on a support selected from the group consisting of molecular sieves, alumina, activated carbons, and silica gel; silver impregnated zeolite selected from the group consisting of faujasites (13X, CaX, NaY, CaY, and ZnX), chabazites, clinoptilolites and LTA (3A, 4A, 5A) zeolites; sulfur or a metal sulfide on an activated carbon support or an activated alumina support; or a metal sulfide, metal oxide, or metal carbonate on a support, the metal is selected from the group consisting of copper, silver, gold, antimony, lead, and manganese, and the support selected from the group consisting of activated alumina, clay, or activated carbon.
10. The process of claim 1 further comprising reducing a viscosity of the at least the portion of the coal tar stream before removing the at least one contaminant.
11. The process of claim 10 wherein the viscosity is reduced by mixing the at least the portion of the coal tar fraction with a solvent.
12. The process of claim 1 further comprising processing at least one of the fractions to produce at least one product.
13. The process of claim 12 wherein the at least one fraction is processed by at least one of hydrotreating, hydrocracking, fluid catalytic cracking, alkylation, transalkylation, oxidation, or hydrogenation.
14. The process of claim 1 wherein the at least one contaminant is removed before the at least the portion of the coal tar stream is separated into the at least two fractions.
15. The process of claim 1 wherein the at least one contaminant is removed after the at least the portion of the coal tar stream is separated into the at least two fractions.
16. A process for removing at least one contaminant from coal tar comprising:
pyrolyzing a coal feed into a coal tar stream and a coke stream;
removing at least one contaminant from at least a portion of the coal tar stream by extraction with an extraction agent or adsorption with an adsorbent to form a treated coal tar stream having a reduced level of the at least one contaminant, the extraction agent comprising at least one of amphiphilic block copolymers, inclusion complexes of poly(methyl methacrylate) and polycyclic aromatic hydrocarbons, cyclodextrins, functionalized cyclodextrins, and cyclodextrin-functionalized polymers, the adsorbent comprising exfoliated graphite oxide, thermally exfoliated graphite oxide or intercalated graphite compounds, and the at least one contaminant comprising nitrogen heterocyclic aromatics, oxygen heterocyclic aromatics, and sulfur heterocyclic aromatics:
separating the coal tar portion into at least two fractions: and processing at least one of the fractions to produce at least one product.
17. The process of claim 16 wherein the extraction agent comprises the amphiphilic block copolymer, and wherein the amphiphilic block copolymer comprises at least two blocks selected from polyethylene oxide blocks, polypropylene oxide blocks, butylene oxide blocks, silicone blocks, urethane blocks, polyurethane ionomer blocks, acrylate ionomer blocks, polymethylacryate blocks, polyacrylic acid blocks, and polyvinylidene chloride blocks.
18. The process of claim 16 wherein the extraction agent further comprises an ionic liquid, or a supercritical fluid, or both.
19. The process of claim 16 further comprising reducing a viscosity of the coal tar fraction before removing the at least one contaminant.
20. The process of claim 16 wherein the at least one fraction is processed by at least one of hydrotreating, hydrocracking, fluid catalytic cracking, alkylation, transalkylation, oxidation, or hydrogenation.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US14/472,263 US20150136660A1 (en) | 2013-11-19 | 2014-08-28 | Process for removing a contaminant from coal tar |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US201361905895P | 2013-11-19 | 2013-11-19 | |
US14/472,263 US20150136660A1 (en) | 2013-11-19 | 2014-08-28 | Process for removing a contaminant from coal tar |
Publications (1)
Publication Number | Publication Date |
---|---|
US20150136660A1 true US20150136660A1 (en) | 2015-05-21 |
Family
ID=53172218
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US14/472,263 Abandoned US20150136660A1 (en) | 2013-11-19 | 2014-08-28 | Process for removing a contaminant from coal tar |
Country Status (3)
Country | Link |
---|---|
US (1) | US20150136660A1 (en) |
CN (1) | CN105705612A (en) |
WO (1) | WO2015077031A1 (en) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105296002A (en) * | 2015-11-17 | 2016-02-03 | 中国五环工程有限公司 | Method for producing fuel oils by hydrogenation after coal tar cleaning and phenol extraction and system thereof |
CN107081168A (en) * | 2016-02-12 | 2017-08-22 | 现代自动车株式会社 | The method for preparing zeolite catalyst |
CN108473877A (en) * | 2015-12-28 | 2018-08-31 | 艺康美国股份有限公司 | The method of the by-product formed in dispersion Dilution steam system |
WO2020115101A1 (en) * | 2018-12-05 | 2020-06-11 | Total Marketing Services | Method for separating polymers in a hydrocarbon mixture |
WO2020190949A1 (en) * | 2019-03-18 | 2020-09-24 | Terrapower, Llc | Mesophase pitch for carbon fiber production using supercritical carbon dioxide |
US10981153B2 (en) | 2016-02-12 | 2021-04-20 | Hyundai Motor Company | Catalyst and method for preparing catalyst |
JP2021063223A (en) * | 2019-10-11 | 2021-04-22 | 南京大学 | Porous cyclodextrin polymer |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN106995719B (en) * | 2016-01-26 | 2019-02-22 | 中科合成油技术有限公司 | The method of organic matter in extracting coal directly-liquefied residue and thus obtained organic matter extract |
CN107055742B (en) * | 2017-05-23 | 2020-09-08 | 航天凯天环保科技股份有限公司 | Desalination method and system for supercritical water oxidation of organic wastewater |
CN112812800B (en) * | 2020-12-23 | 2022-09-23 | 山东科技大学 | Method for extracting and separating alkaline nitride from coal tar by using proton type ionic liquid |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2977299A (en) * | 1957-10-15 | 1961-03-28 | Allied Chem | Production of chemical products from coal products |
US4303531A (en) * | 1978-11-28 | 1981-12-01 | Koei Chemical Co., Ltd. | Method for adsorbing and recovering phenols |
US4375402A (en) * | 1980-08-26 | 1983-03-01 | Occidental Research Corporation | Pyrolysis process |
US5098793A (en) * | 1988-09-29 | 1992-03-24 | Uop | Cyclodextrin films on solid substrates |
US5707528A (en) * | 1996-05-20 | 1998-01-13 | Berry; William Wesley | System and process for treating organic-contaminated aqueous waste streams |
US5792361A (en) * | 1996-03-19 | 1998-08-11 | International Paper Company | Method for treatment of an aqueous waste material |
US7429330B2 (en) * | 2001-08-27 | 2008-09-30 | Calgon Carbon Corporation | Method for removing contaminants from fluid streams |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3862026A (en) * | 1971-09-28 | 1975-01-21 | Gordon Charles Friend | Adsorption of n-paraffins with graphite-alumina pellets |
US3928579A (en) * | 1974-11-25 | 1975-12-23 | Warner Lambert Co | Process for the purification of coal tar |
US4409094A (en) * | 1980-08-08 | 1983-10-11 | Massachusetts Institute Of Technology | Process for detoxifying coal tars |
US7264640B2 (en) * | 2003-06-03 | 2007-09-04 | Southwest Research Institute | Method for improving the performance of engines powered by liquid hydrocarbon fuel |
US7658901B2 (en) * | 2005-10-14 | 2010-02-09 | The Trustees Of Princeton University | Thermally exfoliated graphite oxide |
EP1911737A1 (en) * | 2006-10-12 | 2008-04-16 | Kocat Inc. | Process for preparing an organic acid or its derivatives using a homogeneous MC-Type catalyst an O2/CO2 mixture |
CN101838549B (en) * | 2010-06-17 | 2013-01-30 | 湖南长岭石化科技开发有限公司 | Method for preprocessing coal tar |
CN101912693B (en) * | 2010-07-29 | 2012-08-22 | 河南宝硕焦油化工有限公司 | Equipment and method for separating indole and biphenyl from wash oil fraction |
-
2014
- 2014-08-28 US US14/472,263 patent/US20150136660A1/en not_active Abandoned
- 2014-11-06 WO PCT/US2014/064201 patent/WO2015077031A1/en active Application Filing
- 2014-11-06 CN CN201480061331.4A patent/CN105705612A/en active Pending
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2977299A (en) * | 1957-10-15 | 1961-03-28 | Allied Chem | Production of chemical products from coal products |
US4303531A (en) * | 1978-11-28 | 1981-12-01 | Koei Chemical Co., Ltd. | Method for adsorbing and recovering phenols |
US4303531B1 (en) * | 1978-11-28 | 1988-08-23 | ||
US4375402A (en) * | 1980-08-26 | 1983-03-01 | Occidental Research Corporation | Pyrolysis process |
US5098793A (en) * | 1988-09-29 | 1992-03-24 | Uop | Cyclodextrin films on solid substrates |
US5792361A (en) * | 1996-03-19 | 1998-08-11 | International Paper Company | Method for treatment of an aqueous waste material |
US5707528A (en) * | 1996-05-20 | 1998-01-13 | Berry; William Wesley | System and process for treating organic-contaminated aqueous waste streams |
US7429330B2 (en) * | 2001-08-27 | 2008-09-30 | Calgon Carbon Corporation | Method for removing contaminants from fluid streams |
Non-Patent Citations (2)
Title |
---|
Lin et al. Adsorption of phenol and its derivatives from water using synthetic resins and low-cost natural adsorbents: A review. Journal of Environmental Management, 90 (2009) 1336-1349. * |
Yamasaki et al. Efficient phenol removal of wastewater from phenolic resin plants using crosslinked cyclodextrin particles. J. Chem Technol Biotechnol, 81 (2006) 1271-1276. * |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105296002A (en) * | 2015-11-17 | 2016-02-03 | 中国五环工程有限公司 | Method for producing fuel oils by hydrogenation after coal tar cleaning and phenol extraction and system thereof |
CN108473877A (en) * | 2015-12-28 | 2018-08-31 | 艺康美国股份有限公司 | The method of the by-product formed in dispersion Dilution steam system |
US10604431B2 (en) | 2015-12-28 | 2020-03-31 | Ecolab Usa Inc. | Method to disperse byproducts formed in dilution steam systems |
CN107081168A (en) * | 2016-02-12 | 2017-08-22 | 现代自动车株式会社 | The method for preparing zeolite catalyst |
US10981153B2 (en) | 2016-02-12 | 2021-04-20 | Hyundai Motor Company | Catalyst and method for preparing catalyst |
WO2020115101A1 (en) * | 2018-12-05 | 2020-06-11 | Total Marketing Services | Method for separating polymers in a hydrocarbon mixture |
FR3089517A1 (en) * | 2018-12-05 | 2020-06-12 | Total Marketing Services | Method of separating polymers from a mixture of hydrocarbons |
WO2020190949A1 (en) * | 2019-03-18 | 2020-09-24 | Terrapower, Llc | Mesophase pitch for carbon fiber production using supercritical carbon dioxide |
US11434429B2 (en) | 2019-03-18 | 2022-09-06 | Terrapower, Llc | Mesophase pitch for carbon fiber production using supercritical carbon dioxide |
US11725146B2 (en) | 2019-03-18 | 2023-08-15 | Terrapower, Llc | Mesophase pitch for carbon fiber production using supercritical carbon dioxide |
JP2021063223A (en) * | 2019-10-11 | 2021-04-22 | 南京大学 | Porous cyclodextrin polymer |
Also Published As
Publication number | Publication date |
---|---|
WO2015077031A1 (en) | 2015-05-28 |
CN105705612A (en) | 2016-06-22 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20150136660A1 (en) | Process for removing a contaminant from coal tar | |
US9193921B2 (en) | Hydrocracking process for a hydrocarbon stream | |
US9193644B2 (en) | Process for selectively dealkylating aromatic compounds | |
US9222034B2 (en) | Process for removing a product from coal tar | |
EP3924451A1 (en) | Systems and methods including hydroprocessing and high-severity fluidized catalytic cracking for processing petroleum-based materials | |
US20150136654A1 (en) | Process for treatment of pitch from coal tar | |
US20150136696A1 (en) | Process for removing aromatics from water used in processing coal tar | |
WO2022019939A1 (en) | Systems and processes for direct converting distillate fractions of crude oil to olefins | |
WO2015076973A1 (en) | Process for pyrolysis of a coal feed | |
US9162943B2 (en) | Method of converting a coal to chemicals | |
US20150141726A1 (en) | Process for producing olefins from a coal feed | |
US20150136650A1 (en) | Process for removing mercury from a coal tar product | |
WO2015077045A1 (en) | Process for hydrotreating a coal tar stream | |
US20150136656A1 (en) | Process for pyrolysis of coal | |
US9162952B2 (en) | Process for purifying products from coal tar | |
US20150136653A1 (en) | Process for pyrolysis and gasification of a coal feed | |
US20150136580A1 (en) | Process for pyrolyzing coal using a recycled hydrogen donor | |
US20150136658A1 (en) | Process for removing ash and heavy hydrocarbons from coal tar | |
WO2015076979A1 (en) | Process for hydrotreating a coal tar stream | |
US11866397B1 (en) | Process configurations for enhancing light olefin selectivity by steam catalytic cracking of heavy feedstock | |
US20150136655A1 (en) | Process for producing hydrogen-rich coal tar | |
CN105722955A (en) | Hydrotreating process and multifunction hydrotreater related applications |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: UOP LLC, ILLINOIS Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:BEDARD, ROBERT L.;GORAWARA, JAYANT K.;JAN, DENG-YANG;AND OTHERS;SIGNING DATES FROM 20140829 TO 20140903;REEL/FRAME:034079/0818 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |