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
  • C10G7/00—Distillation of hydrocarbon oils
• • 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
  • C10G1/006—Combinations of processes provided in groups C10G1/02 - C10G1/08
• • 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
  • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
• • 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
  • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
  • C10G1/086—Characterised by the catalyst used
• • 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
  • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
  • C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
  • C10L1/00—Liquid carbonaceous fuels
  • C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
• • 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
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1003—Waste materials
• • 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
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/04—Diesel oil

Definitions

• the present invention relates to a process for the production of diesel oil from hydrocarbon-containing residues in an oil circulation with solids separation and product distillation for the diesel product
• FIG. 2 shows a schematic representation of the system from FIG. 1
• an emulsion container 2 is arranged on the suction side of a high-performance chamber mixer 1, which has three inlet openings. by an entry system 3, which acts crushing and dosing, adjacent to the entry container 2
• the other two openings on the entry vessel 2 are a Kreislaufkatalysatorol- supply 10 from a Olsammelbehalter 15 and a Sammelkatalysatorol supply 11 from an oil collecting container 15, which is arranged at the outlet 29 of this ⁇ lsammeJ seers 15. This makes it possible for the catalyst oil to also keep the lime residues in circulation.
• a pressure line 12 On the pressure side of the high-performance chamber mixer 1, a pressure line 12 is attached. It directs the product vapor-oil mixture produced in the high-performance chamber mixer 1 into an evaporator 14. This has a distribution channel 13 which divides the incoming oil-vapor mixture into a plurality of partial streams through perforated plates in an open-ended annular die forming the wall wet and leads to the largest possible surface of the liquid in the evaporator 14.
• the entry system 3 is controlled by a level control container 16, which indicates and regulates the level in the oil reservoir 15, on and off or in the speed regulated.
• a pump 17 is arranged, which directs a small amount of oil to the entry system 3 in order to protect it from blockages.
• the product vapor is purified in the distillation column 18 by fractional distillation of the entrained oil particles and condensed in the condenser 19.
• the thereby incurred in the condensation of water are retained in the condenser 19 by a partition wall due to their higher specific gravity on the input side.
• the water content passes into a pH measuring container 20 by exchange with the product located there with the water settling down.
• a pH measuring probe 23 In the pH measuring container 20 is a pH measuring probe 23 and a conductivity probe 22.
• a certain amount of water is discharged into a product water tank 21 and discharged from there into a sewer.
• the lighter product diesel or fuel oil passes through the baffle in the condenser on the output side in a product line 24, wherein vaporous product components over a line 26 also as the product in the product line 24 into a product container 25 arrive.
• a small portion of the product passes via the line 24, regulated via a return valve 28, back into the distillation column 18 in one of the upper floors 27th
• the control is set so that the amount controls the return in the column. This produces a different product quality for summer diesel with an average boiling point of 290 0 C, for winter diesel with an average boiling point of 27O 0 C and kerosene with an average boiling point of 240 0 C.
• a vacuum pump 37 which keeps the entire system at negative pressure.
• the sucked gas is added to the generator as intake air or purified in a catalytic exhaust air purification. As gases which are sucked out of the plant fall from the biological substances derived carbon dioxide and possibly resulting from leaks small Gasmenge ⁇ on.
• the vacuum pump controls the amount of entry and the amount of discharge of non-reactive, inorganic residues that are discharged at the bottom of the system.
• the non-reactive components of the input material and the catalyst exchanging with the ions and the added lime or soda-forming salts pass through a control valve 30 and a hot sludge pump 31 into a heat chamber 32.
• This is electrically heated to 55O 0 C and has on the inside a heat-resistant evaporation vessel with the sludge inlet, a vapor return to the evaporator and a screw discharge 33 for the heated inorganic substances, which reach a remind ⁇ tands electricer 34. This is on average 1 to 3% of the input material.
• the substances collected in the residue container 34 are subsequently mixed with the water of the container 21.
• the substances settling in the suspension, metal, glass and ceramic, are separated and the suspension is filtered.
• the filter residue is again a usable catalyst.
• the liquid contains the salts formed and is passed into the wastewater.
• the containers have relief and pressure equalization lines, such as the feed tank 2, through a venting chamber with check valve 36 with the distillation column - A -
• a high-performance chamber mixer 1 with an electrical output of 200 kW draws from a collecting tank 2 with a volume of 800 I, the solids from the Correau pump of Correau Paris, a Zahnradzerklein réelles- and metering pump with 37 kW.
• the container arranged above it has a capacity of 2 m 3 .
• the connection line is DN50.
• the connecting lines between the collecting container 2 and the oil collecting container 15 are relatively small in order to allow a high mixing effect in the collecting container at high oil discharge speed and controlled negative pressure. They have a diameter of 1, 5 inches and valves that regulate the negative pressure in the reservoir 2, depending on the material located on the entry 3 material.
• the discharge line with check valve 36 has a diameter of 3/4 inch.
• the evaporation tank 14 has a capacity of 2 m 3 and a distribution channel 13 with a width of 80 mm and three rows of holes with a hole diameter of 8 mm, the inner and outer row of holes having oblique holes from the center to the wall and the interior.
• the arranged underneath oil reservoir 15 has a volume of 1, 5 m 3 and the level tank has a volume of 100 liters.
• the distillation column 18 has 15 bell bottoms, each with 52 bells with a diameter of 600 mm.
• the condenser 19 has a volume of 300 liters.
• the discharge system has the control valve 30 DN50 with a hot sludge pump without plastic parts and is connected to the heat chamber 32, a heating oven from Nabertherm 15 kW power, and a steam pipe 35 to the evaporator 14 with a diameter of 1, 5 inches, isolated and with Provided condensation loops.
• the screw discharge 33 is a screw with a diameter of 200 mm and a closure shell over the connection of the residue container 34 with a volume of 1 m 3 .
• the conduit to the pH container 20 has a diameter of 1.5 inches and the p-container has a volume of 0.5 m 3 with a conductivity probe 22 and a pH meter 23.
• the water collection container 21 has a volume of 1 m 3 .
• the device for carrying out the method is explained in FIG.
• an input container 102 is arranged, which has inlet openings.
• the collection container 104 At the upper end of the container there is the first inlet opening, the collection container 104, which through an entry system 103, which has gears and a Dosierani and adjacent to the entry container 102.
• the input ports, dry residue 105, residue oil from the plant or residue 106, lime or soda as neutralizer 107, and a catalyst 108 in the mixing hopper 109 are connected to the feed system 103 through a mixing hopper 109 and a header 104. Both the mixing funnel 109 and the collecting container 104 are equipped with vibrators.
• the other two openings on the feed tank 102 are the recycle catalyst oil feeds 110 from an oil receiver 115 and the cumulative catalyst oil feeds 11 1 from an oil receiver 115 located at the outlet 129 of this oil receiver 115.
• a pressure line 112 is attached on the pressure side of the high-performance chamber mixer 101. It connects the high-performance chamber mixer 101 with an evaporator 1 14. This has a distribution channel 113, which is equipped on the inside with perforated plates in an annular nozzle with an open end.
• the entry system 103 is connected to a level control container 16. This contains a level probe. At the lower end of the level control container 116, a pump 117 is arranged, which has a kausu ⁇ gs effet to the entry system 103.
• the evaporator 114 is connected to a distillation column 118 having a plurality of trays 127. At the upper end of the distillation column 118, the condenser 119 is arranged, which has a partition wall inside. The condenser 119 has a connection on the input side to a pH measuring container 120. In the container, a conductivity probe 122, which is electronically connected to a water drainage valve, and a pH measuring probe 123 are mounted.
• conduits 124 and 126 On the side of the condenser 119, which is opposite to the input side, there are provided at the bottom and top of conduits 124 and 126, which are connected to a product container 125.
• a return valve 128 In the product line 124, a return valve 128 is arranged, which is connected to a connecting line to the distillation column 118.
• the return valve 128 has with an electronic control connection, which is set to a temperature measurement. This regulation has the ads summer diesel, winter diesel and kerosene.
• the condenser 1 19 has on the cooling side connection to a recool 138 with circulating water pump. After the product container 125 is a vacuum pump 137, which is thus connected to all parts of the system.
• control valve 130 is disposed at the lower end of the oil collecting tank 115. This is connected to a hot slurry pump 131 and a heat chamber 132. This is located in an electrically heated oven and has next to the entrance of the hot slurry pump 131, a steam pipe 135th
• This line is also insulated and has condensate loops with drain taps and terminates in the evaporator vessel 114.
• the heating chamber 132 has on the exit side a screw exit 133 which is connected to a residue tank 134.
• the residue container 134 is followed by a suspension chamber having a connecting line to the product water tank 121 and has two outputs. One outlet on the upper side is connected to a filter press suitable for catalyst slurry, and the lower side is connected to a recyclable material container for ceramics, metal and gas.
• the containers have relief and pressure equalization lines, such as the feed tank 102 which is connected to the distillation column 118 through a bleed chamber with check valve 136. Furthermore, all heat-conducting parts are doubly insulated with an alumina fiber mat on the surface and an insulating mat over it. Outside, a cover plate is arranged, which is formed on the turbine as a closed chamber, which can withstand a small overpressure.
• a high-performance chamber mixer 101 with an electrical line of 200 kW has a connecting line with a reservoir 102 with a volume of 800 I. This has a connection line up with the Correau pump from Correau Paris, a Zahnradzerkleine- tion and metering pump with 37 kW.
• the container arranged above it has a capacity of 2 m 3 .
• the connection line is DN50.
• the connecting pipes between the feed tank 102 and the oil collecting tank 1 15 are relatively small and have a diameter of 1, 5 inches and valves that regulate the negative pressure in the hopper 102, depending on the material at the level of the entry system 103 material.
• the discharge line with check valve 136 has a diameter of 3/4 inch.
• the evaporator 114 has a capacity of 2 m 3 and a distribution channel 1 13 with a width of 80 mm and three rows of holes with a hole diameter of 8 mm, the inner and outer row of holes oblique holes from the center away from the wall and the interior.
• the oil collecting tank 115 disposed thereunder has a volume of 1.5 m 3 and the level control tank has a volume of 100 liters.
• the distillation column 1 18 has 15 bell bottoms, each with 52 bells with a diameter of 600 mm.
• the condenser 19 has a volume of 300 liters.
• the discharge system has the control valve 130 DN50 with a hot slurry pump 131 without plastic parts and is connected to the heat chamber 132, a heating oven from Nabertherm with 15 kW power, and a steam pipe 135 to the evaporator 114 with a diameter of 1, 5 inches, isolated and provided with condensation loops.
• the screw discharge 133 is a screw having a diameter of 200 mm and a closure shell via the connection of the residue container 134 with a volume of 1 m 3 .
• the line to the pH measuring container 120 has a diameter of 1, 5 inches and the pH measuring container has a volume of 0.5 m 3 with conductivity probe 122 and pH probe 123.
• the product water tank 121 has a volume of 1 m 3 .

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• Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Engineering & Computer Science (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Life Sciences & Earth Sciences (AREA)
• Wood Science & Technology (AREA)
• Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
• Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)

Applications Claiming Priority (2)

Publications (1)

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ID=38535585

Family Applications (1)

Country Status (10)

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• 2007
  • 2007-04-04 EP EP07722181A patent/EP2134812A1/de not_active Withdrawn
  • 2007-04-04 WO PCT/DE2007/000623 patent/WO2008061484A1/de active Application Filing
  • 2007-04-10 BR BRPI0701999-8A patent/BRPI0701999A2/pt not_active IP Right Cessation
  • 2007-04-24 CN CNA2007101012379A patent/CN101186838A/zh active Pending
  • 2007-05-25 MX MX2007006278A patent/MX2007006278A/es active IP Right Grant
  • 2007-11-14 US US11/939,817 patent/US20080116116A1/en not_active Abandoned
  • 2007-11-15 CA CA002610624A patent/CA2610624A1/en not_active Abandoned
  • 2007-11-19 RU RU2007142659/04A patent/RU2447131C2/ru not_active IP Right Cessation
  • 2007-11-19 JP JP2007299152A patent/JP2008133471A/ja active Pending
  • 2007-11-20 KR KR1020070118672A patent/KR20080045654A/ko not_active Application Discontinuation

Non-Patent Citations (1)

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