WO2008038731A1 - procédé de craquage thermique, réacteur de craquage thermique et appareil de craquage thermique pour pétrole lourd - Google Patents
procédé de craquage thermique, réacteur de craquage thermique et appareil de craquage thermique pour pétrole lourd Download PDFInfo
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- WO2008038731A1 WO2008038731A1 PCT/JP2007/068853 JP2007068853W WO2008038731A1 WO 2008038731 A1 WO2008038731 A1 WO 2008038731A1 JP 2007068853 W JP2007068853 W JP 2007068853W WO 2008038731 A1 WO2008038731 A1 WO 2008038731A1
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- reaction tank
- superheated steam
- oil
- petroleum
- heavy
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Classifications
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- 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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
- B01J4/002—Nozzle-type elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00004—Scale aspects
- B01J2219/00006—Large-scale industrial plants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/00029—Batch processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/00031—Semi-batch or fed-batch processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/00038—Processes in parallel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00121—Controlling the temperature by direct heating or cooling
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00182—Controlling or regulating processes controlling the level of reactants in the reactor vessel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00245—Avoiding undesirable reactions or side-effects
- B01J2219/00247—Fouling of the reactor or the process equipment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/19—Details relating to the geometry of the reactor
- B01J2219/194—Details relating to the geometry of the reactor round
- B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
- B01J2219/1946—Details relating to the geometry of the reactor round circular or disk-shaped conical
-
- 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
- C10G2300/80—Additives
- C10G2300/805—Water
- C10G2300/807—Steam
Definitions
- the present invention relates to a method for pyrolysis treatment of heavy petroleum oil, a pyrolysis reaction tank used therefor, and a pyrolysis treatment apparatus including the pyrolysis reaction tank.
- Heavy petroleum oil or residual oil with low added value such as petroleum asphalt with a high sulfur content, has a great impact on the environment when used as fuel. For this reason, such heavy petroleum oils (including residual oils; the same shall apply hereinafter) are decomposed and converted into various useful industrial raw materials.
- One method is thermal decomposition. Processing
- FIG. 14 shows a schematic perspective view of a reaction tank used in a conventional method for pyrolyzing heavy petroleum oil.
- the reaction vessel 106 is a cylindrical reaction vessel main body or body) 116, and a bottom-shaped hollow vessel having a blowing nozzle 114 communicating with the inside of the reaction vessel 106. The bottom is sunk. Superheated steam is blown from the blowing nozzle 114 in the state where the heavy petroleum oil is filled in the reaction tank 106. The role of superheated steam blown from the bottom of the reactor is the heating and decomposition products of petroleum heavy oil. Is promptly discharged.
- Patent Document 1 Japanese Patent Publication No. 7-116450
- Patent Document 2 Japanese Patent Publication No. 54-15444
- Patent Document 3 Japanese Patent Publication No.57-15795
- Patent Document 4 Japanese Patent Publication No. 63-38076
- the present invention improves the superheated steam blown into the reaction vessel causing the drawbacks of the above prior art, and improves the superheated steam in the reaction vessel to a preferable dispersion state, thereby improving the reaction vessel.
- a method for pyrolysis treatment of heavy petroleum oil that can prevent coke adhesion and prevent clogging in the reaction vessel outlet cracking gas piping, and can produce a high-quality and homogeneous pitch, and thermal cracking used therefor It is an object of the present invention to provide a reaction tank and a thermal decomposition treatment apparatus provided with the thermal decomposition reaction tank.
- the method of pyrolysis treatment of heavy petroleum oil of the present invention (hereinafter sometimes simply referred to as “the method of thermal decomposition treatment of the present invention”) is heated to 450 ° C. or higher in a heating furnace,
- the reaction vessel having a cylindrical body at least, the reaction vessel
- the method of thermal decomposition treatment of heavy petroleum oil in which superheated steam at 400 to 700 ° C. is blown from the bottom of the oil so that the superheated steam is brought into direct contact with the petroleum heavy oil and thermally decomposed into oil and pitch.
- the superheated steam When the superheated steam is blown from the bottom of the reaction tank, the superheated steam is blown inside the reaction tank so as to generate a swirling flow around the axis of the reaction tank body.
- the superheated steam is blown so that the superheated steam generates a swirling flow around the axis of the reaction tank body, thereby turning inside the reaction tank. Stirring effect by the flow is born, and the dispersion state of superheated steam is improved. As a result, the rapid discharge of the decomposition products and the promotion of the decomposition of the heavy petroleum oil can be achieved, so that a high-quality and uniform pitch can be produced.
- the superheated steam is blown from the bottom of the reaction tank through one or two or more blow holes that communicate with the inside of the reaction tank provided at the bottom of the reaction tank.
- the superheated steam is blown from the blowing port in a direction perpendicular to the axis of the reaction vessel body and parallel to or above the plane including the blowing port and on the outer wall of the reaction vessel. Angle formed by the line ⁇ force Directed in the direction of more than 0 ° and less than 90 °.
- the superheated steam can generate a swirling flow around the axis of the reaction vessel body.
- the angle ⁇ formed is preferably 20 ° or more and 60 ° or less.
- the petroleum heavy oil pyrolysis reaction tank of the present invention (hereinafter sometimes simply referred to as “the pyrolysis reaction tank of the present invention” or “the reaction tank of the present invention”) is used in a heating furnace. After heating to 450 ° C or higher, 400 to 700 ° C superheated steam is blown from the bottom of the reaction tank into at least the petroleum heavy oil introduced into the cylindrical reaction tank. And the excess The reaction vessel for use in a method for pyrolysis treatment of petroleum heavy oil in which thermal steam is directly contacted with the petroleum heavy oil to thermally decompose into oil and pitch,
- steam blowing means is arranged to blow the superheated steam so that a swirling flow is generated around the axis of the reaction tank body inside the reaction tank. It is characterized by.
- the steam blowing means as described above is arranged, so that the superheated steam generates a swirling flow around the axis of the reaction tank body, and stirring is performed.
- This produces an effect and improves the dispersion state of the superheated steam.
- the rapid release of cracked products and the acceleration of the cracking of heavy petroleum oils can be achieved, and it is possible to produce high-quality and uniform pitches.
- the superheated steam spreads inside while being uniformly dispersed, the superheated steam is not blown out, so that quick discharge is achieved, the entry is reduced, and the coke in the reaction tank outlet decomposition gas piping is reduced. Suppression of adhesion and prevention of clogging can be achieved.
- the reaction tank provided at the bottom of the reaction tank communicates with the inside of the reaction tank through one or two or more pipe-shaped blowing nozzles that communicate with each other through the blowing port.
- the blowing nozzle is parallel to or above the plane perpendicular to the axis of the reaction vessel body and including the blowing port, and the reaction
- the angle between the outer wall of the tank and the normal on the plane ⁇ force is directed in the direction exceeding 0 ° and 90 ° or less, and directed in the direction of 20 ° or more and 60 ° or less preferable.
- the petroleum heavy oil pyrolysis apparatus of the present invention at least converts the petroleum heavy oil to 450 °.
- a heating furnace heated to C or higher and a heated petroleum heavy oil are introduced, and a superheated steam of 400 to 700 ° C is blown from the bottom so that the superheated steam is directly applied to the petroleum heavy oil.
- a thermal decomposition treatment apparatus comprising: a reaction tank that is thermally decomposed into oil and pitch by contact; The reaction tank is a pyrolysis reaction tank for petroleum heavy oil according to the present invention.
- the reaction tank has a configuration in which superheated steam is blown in a swirling flow from the bottom of the reaction tank.
- the superheated steam is uniformly dispersed inside, and the rapid discharge of cracked products and the promotion of the cracking of petroleum heavy oil are thereby achieved. For this reason, the coke adherence at the reaction vessel outlet line or the like is suppressed by the force S to suppress clogging and produce a high-quality uniform pitch.
- FIG. 1 is a flow sheet for explaining the overall configuration of a thermal heavy oil pyrolysis method or thermal cracking apparatus according to the present invention.
- FIG. 2 is a schematic perspective view showing an exemplary embodiment of the thermal decomposition reaction tank of the present invention used in the thermal decomposition method or apparatus for heavy petroleum oil of the present invention.
- FIG. 3 is a bottom view of the thermal decomposition reaction tank shown in FIG. 2.
- FIG. 4 is a cross-sectional view taken along the arrow D-D in the vicinity of the bottom of the pyrolysis reactor shown in FIG. 3.
- the left half is shown. Is omitted.
- FIG. 5 is a bottom view of the thermal decomposition reaction tank shown in FIG. 14 for use in a conventional method for pyrolyzing heavy petroleum oil.
- FIG. 6 is a cross-sectional view of D′—D ′ near the bottom of the thermal decomposition reaction tank shown in FIG. 5. For convenience of explanation, only one blowing nozzle is shown, and the left half Is omitted.
- FIG. 7 is a schematic perspective view for explaining the calculation part of the volume fraction of gas in the thermal decomposition reaction tanks of Examples and Comparative Examples!
- FIG. 8 is a graph showing the results of the effect confirmation study for the thermal decomposition reaction tanks of Examples and Comparative Examples, and (1) plots the calculation results of the X coordinate of the TL1 surface.
- FIG. 9 shows the results of the effect confirmation study on the pyrolysis reaction tanks of Examples and Comparative Examples! It is a graph, (1) Plotted calculation result of Y coordinate of TL1 surface.
- FIG. 10 A graph showing the results of the effect confirmation study on the pyrolysis reactors of the example and the comparative example! (2) The calculation result of the X coordinate of the surface 1.5m above TL1 It is a plot.
- FIG. 11 A graph showing the results of the effect confirmation study on the pyrolysis reactors of the example and comparative example! (2) Y coordinate calculation result of the surface 1.5m above TL1 It is a plot.
- FIG. 12 is a graph showing the results of the effect confirmation study for the thermal decomposition reaction tanks of the example and the comparative example. (3) Plotted the calculation result of the X coordinate of the surface 3 m above TL1 Is a thing
- FIG. 13 is a graph showing the results of the effect confirmation study for the pyrolysis reaction tanks of the examples and comparative examples. (3) Y-coordinate calculation results of the surface 3 m above TL1 are plotted. Stuff
- FIG. 14 is a schematic perspective view showing a reaction tank used for a conventional thermal decomposition method for heavy petroleum oil.
- FIG. 1 is a flow sheet for explaining the overall configuration of a petroleum heavy oil pyrolysis treatment method or pyrolysis treatment apparatus of the present invention.
- the raw material oil (petroleum heavy oil) sent from the raw material tank 1 is preheated to about 350 ° C by the raw material preheating furnace 2 and enters the distillation column 3.
- the cracked oil that falls to the bottom of the tower as recycled oil is mixed with the heavy-end fraction.
- the ratio of this recycled oil to the raw material is 0.05-0.25, preferably 0.10—0.20.
- the raw material oil mixed with the recycled oil is sent to a tubular heating furnace (heating furnace) 4.
- Tubular heating In Hito 4 the raw oil is 480-500. C, preferably 490-500. Heat up to the temperature of C and advance the arc.
- the outlet pressure in the tubular furnace 4 is about normal pressure to about 0.4 MPa, and the reaction time is usually about 0.5 to 10 minutes, preferably about 2 to 5 minutes.
- the high-temperature pyrolysis product (petroleum heavy oil) obtained in the tubular heating furnace 4 is flushed to a predetermined reaction tank (pyrolysis reaction tank) 6, 6 'via a switching valve 5.
- a predetermined reaction tank pyrolysis reaction tank
- the raw material oil is partially applied in advance (preliminary application) through the switching valve 7 from the bottom of the distillation column 3.
- the amount of this tension is 5 to 18% by volume, preferably 10 to 15% by volume of the total amount of the reactors 6, 6 ′.
- the temperature of the raw oil for the preliminary filling is about 340 ° C.
- the change-over valves 5 and 7 are operated at regular intervals, respectively, and the raw oil for pre-filling and the pyrolysis product from the tubular furnace 4 are periodically supplied to the two reaction vessels 6 and 6 ', respectively. Paste alternately. By such a periodic operation, the thermal decomposition treatment in the reaction tank of the thermal decomposition treatment product continuously supplied from the tubular heating furnace 4 is continuously performed.
- the reaction tanks 6, 6 ' are containers having a cylindrical shape with a cylindrical bottom and a concave bottom (a shape in which the cross-sectional diameter gradually decreases toward the end).
- a raw material inlet, a heat medium gas inlet, a cracked gas, cracked oil and heat medium gas outlet, and a residue outlet are provided.
- a stirrer can be installed as needed.
- the time for this one embedding it is preferable to set the time for this one embedding to 50 to 120 minutes, preferably about 60 to 90 minutes.
- the softening point of the residue in the tank hereinafter also simply referred to as “pitch”.
- the reaction time after this stretching is preferably defined as 15% to 45%, preferably 25% to 45% of the stretching time.
- the temperature of the superheated steam supplied to the reaction vessels 6, 6 ' is 400 to 700 ° C, and it is sufficient to use steam having a relatively low temperature. Also, the supply amount is small, and the ratio of 0.08 to 0.15 kg is sufficient as the ratio of the total feed oil supply amount to 1 kg for the tubular heating furnace 4 and the reaction vessels 6 and 6 ′.
- FIG. 2 is a schematic perspective view of an embodiment showing an exemplary aspect of the thermal decomposition reaction tank of the present invention used in the thermal decomposition method or apparatus for heavy petroleum oil of the present invention. .
- the reaction tank (pyrolysis reaction tank) 6 is connected to the cylindrical reaction tank body (or reaction tank body 16) and the bottom of the reaction tank 6, and the reaction tank 6 2 and a bottom portion (or a bottom portion) having a sunk shape provided with squirting nozzles 14a and 14b communicating with each other through the squirting ports 18a and 18b (between TL1 and TL2 in FIG. 2).
- the area with the same inner diameter is called the reaction vessel body, and the area below TL1 in Fig. 2 is called the bottom.
- superheated steam is also blown into the blowing nozzles 14a and 14b with the heavy petroleum oil in the reaction tank 6 (OL in FIG. 2 indicates the liquid level).
- the dimensions shown in FIG. 2 indicate the actual dimensions of the reaction tank used in the examples described later.
- the alternate long and short dash line with the symbol S indicates the center axis S of the body 16 of the reaction tank 6, and the alternate long and two short dashes line with the symbols Ta and Tb indicates the inlet 18a in the reaction tank 6. Or the line which shows the height in which the blowing inlet 18b is located is each represented.
- the symbols Ta and Tb indicate the plane including the corresponding two-dot chain line, and are expressed as the plane Ta and the plane Tb.
- FIG. 3 shows a bottom view of the reaction vessel 6 shown in FIG. 2 (a plan view seen from the bottom side).
- a total of 16 blowing nozzles 14a, 14b are arranged at the bottom of the reaction tank 6, 8 each in two upper and lower stages.
- the axes of the blowing nozzles 14a and 14b are all perpendicular to the central axis S and are straight lines passing through the blowing port 18a or the blowing port 18b (that is, the outer wall of the reaction vessel body 16 in the planes Ta and Tb).
- the normal angle to U is 30 °.
- FIG. 4 is a cross-sectional view taken along the arrow D-D near the bottom of the reaction vessel 6 shown in FIG.
- FIG. 4 is a drawing for explaining the orientation of the blowing nozzles 14a and 14b, only one blowing nozzle 14a is shown, and the other blowing nozzles are not shown. For the same reason, only the right half of the reaction tank 6 is shown, and the left half is not shown.
- the blowing nozzle 14a is perpendicular to the central axis S and is directed parallel to or slightly above the plane Ta including the blowing port 18a.
- the angle directed upward of the blowing nozzle 14a that is, the angle ⁇ formed by the axis of the blowing nozzle 14a and the plane Ta is 0 ° (parallel to the plane Ta). It should be noted that the angle ⁇ formed is the same for the other blowing nozzles 14a and 14b.
- the superheated steam blown into the reaction vessel 6 from here also has a direction in which the angle ⁇ formed with respect to the plane Ta and Tb becomes 0 ° ( It is directed in the direction of arrow C in Figs. 2 and 4.
- FIG. 5 shows a bottom view (a plan view seen from the bottom side) of the reaction vessel 106 shown in FIG.
- blowing nozzles 114 are arranged at the same height (one stage) at the bottom of the reaction tank 106.
- each of the blowing nozzles 114 is directed to the central axis S ′ (in other words, the blow nozzle 114 is perpendicular to the axis of the blowing nozzle 114 and the central axis S ′).
- the angle formed by a straight line passing through the blowing port in the section 116 (that is, the normal to the outer wall of the body section 116 of the reaction vessel 106 in the plane T ′) is 0 ° ⁇ . Since the direction of the blowing nozzle 114 is set in this way, the superheated steam blown from here into the reaction tank 106 is also directed to the central axis S ′.
- FIG. 6 is a cross-sectional view taken along arrow D′-D ′ in the vicinity of the bottom of the reaction vessel 106 shown in FIG.
- FIG. 6 is a drawing for explaining the direction of the blowing nozzle 114, only one blowing nozzle 114 is shown, and the other blowing nozzles are not shown. For the same reason, only the right half of the reaction vessel 106 is shown, and the left half is not shown.
- the blowing nozzle 114 is directed upward with respect to a plane T ′ that is perpendicular to the central axis S ′ and includes the blowing port of the nozzle 114.
- the angle directed upward of the blowing nozzle 114 that is, the angle ⁇ formed by the blowing nozzle 114 and the plane Ta is 45 °.
- the angle ⁇ formed is the same for all of the other blowing nozzles 114.
- Blowing force of superheated steam into the reaction vessel 106 As shown in this conventional example, this blowing is performed when it is made slightly upward (in the direction of the arrow C ') of the central axis S' of the barrel 116 of the reaction vessel 106. The force is bundled near the central axis S ', and a driving force is generated in the direction of arrow ⁇ ⁇ in Fig. 14. Therefore, the behavior of this superheated steam is such that the central part of the reaction tank 106 is blown away, or a heavy oil stagnation part is formed inside the body part 116 of the reaction tank 106. Bias is likely to occur.
- the direction of the blowing nozzles 14a and 14b (synonymous with the "superheated steam blowing direction") described in the present embodiment is merely an example, and in the present invention, The angle is not limited as long as the superheated steam generates a swirling flow around the axis of the reaction vessel body in the reaction vessel. What is necessary is just to select a preferable condition suitably so that it may be in the optimal swirl
- the angle ⁇ between the axis of the blowing nozzles 14a and 14b and the straight line U in Fig. 3 is more than 0 ° and not more than 90 ° in order to incline the direction of the blowing nozzles 14a and 14b. However, it is preferably 20 ° or more and 60 ° or less, more preferably 25 ° or more and 50 ° or less.
- the formed angle ⁇ is too small, the force in the direction of giving the swirling flow to the superheated steam is insufficient, and an appropriate swirling flow is easily generated.
- the formed angle ⁇ is too large, the superheated steam blown from the blow inlets 18a and 18b by the blow nozzles 14a and 14b acts on the inner wall of the reaction tank 6 and sometimes completely collides with it. This is not preferable because the inner wall may be eroded.
- the angle ⁇ between the axis of the blowing nozzle 14a and the plane Ta in Fig. 4 is 0 ° or more and 30 ° or less in order to direct the blowing nozzle 14a slightly upward from parallel.
- the force S is preferably 15 ° or less.
- the power described for the thermal decomposition treatment method, thermal decomposition reaction tank, and thermal decomposition treatment apparatus for petroleum heavy oil of the present invention is configured according to the above-described embodiment.
- the number of blowing nozzles is given as an example in which the number of blowing nozzles is 8 in each of the upper and lower two stages.
- the number of blowing nozzles is not limited to 16. Also, it is possible to divide it into two or more stages, or it can be divided into three or more stages.
- reaction tank of the example a product having a shape 'structure shown in Fig. 2 was used.
- reaction tank of the conventional example the one having the shape 'structure shown in FIG. 14 was used.
- the dimensions of the reaction tank of the comparative example are not shown in FIG. 14, but are the same as the dimensions of the reaction tank of the embodiment shown in FIG. 2 (in FIG. 2, OL is the liquid level, and TL1 is the lower end of the barrel. , TL
- the arrangement of the nozzles 14a and 14b in the reaction tank of the example is as shown in Figs. 3 and 4, and more specifically, the height force of the nozzles 18a and 18b from TL1. 18a is 1.5m, and the inlet 18b is 2.5m.
- the arrangement of the blowing nozzle 114 in the reaction tank of the comparative example is as shown in FIGS. 5 and 6. More specifically, the height of the blowing nozzle 114 from the TL1 is 1 2 • 15 m. Get out.
- each of the blowing nozzles of the example and the comparative example used an inner diameter of 28.4 mm.
- Feed oil (petroleum heavy oil) is fed into a tubular furnace in each of the reaction tanks of the above Examples and Comparative Examples.
- FIG. 7 is a schematic perspective view for explaining the calculation part of the gas volume fraction in the effect confirmation examination for the reaction vessels 6 and 106 of the example and the comparative example.
- FIG. 8 to FIG. 13 are graphs showing the calculation results of the dispersion state in the radial direction of the superheated steam inside the reaction tanks of Examples and Comparative Examples.
- Figure 8 for the X coordinate calculation results for (1) surface (TL1 surface), Figure 9 for the Y coordinate calculation results, and (2) surface (1.5 meters above TL1)
- Fig. 10 shows the calculation result
- Fig. 11 shows the calculation result of the Y coordinate
- Fig. 12 shows the calculation result of the X coordinate of the (3) plane (surface 3m above TL 1)
- Fig. 13 shows the calculation result of the Y coordinate.
- Each is shown in a graph.
- the 0.0 point of the X or Y coordinate is the origin (intersection with the central axes S and S '), and the numerical value of the X or Y coordinate is the distance (unit: m).
- the superheated steam is blown in the swirling flow from the bottom, so that the vicinity of the central part like the reaction tank 106 of the comparative example It can be seen that the superheated steam is uniformly dispersed inside the reaction vessel 6 where no gas blow-through occurs in the reactor.
- This power achieved rapid discharge of cracked products and accelerated decomposition of petroleum heavy oil, resulting in reaction tank 6 and reaction tank 6 outlet line. It can be seen that coke adhesion and clogging at the same time are suppressed, and that a high-quality and uniform pitch can be produced.
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US12/440,424 US8262903B2 (en) | 2006-09-28 | 2007-09-27 | Process, reactor and facility for thermally cracking heavy petroleum oil |
MX2009002395A MX2009002395A (es) | 2006-09-28 | 2007-09-27 | Procedimiento, reactor e instalacion para la pirodesintegracion de aceite pesado de petroleo. |
CA2663639A CA2663639C (en) | 2006-09-28 | 2007-09-27 | Process, reactor and facility for thermally cracking heavy petroleum oil |
CN2007800346313A CN101517040B (zh) | 2006-09-28 | 2007-09-27 | 石油系重质油的热裂解处理方法和热裂解反应槽、以及热裂解处理装置 |
BRPI0717591A BRPI0717591B1 (pt) | 2006-09-28 | 2007-09-27 | método para processamento de craqueamento térmico de óleo de petróleo pesado, bem como recipiente de reação para craqueamento térmico |
EP07828599.6A EP2072603A4 (en) | 2006-09-28 | 2007-09-27 | THERMAL CRACKING METHOD, HEAT CRACKING REACTOR AND HEAT CRACKING APPARATUS FOR HEAVY PETROLEUM |
Applications Claiming Priority (2)
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JP2006-264139 | 2006-09-28 | ||
JP2006264139A JP4951302B2 (ja) | 2006-09-28 | 2006-09-28 | 石油系重質油の熱分解処理方法および熱分解反応槽、並びに熱分解処理装置 |
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PCT/JP2007/068853 WO2008038731A1 (fr) | 2006-09-28 | 2007-09-27 | procédé de craquage thermique, réacteur de craquage thermique et appareil de craquage thermique pour pétrole lourd |
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Country | Link |
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US (1) | US8262903B2 (ja) |
EP (1) | EP2072603A4 (ja) |
JP (1) | JP4951302B2 (ja) |
CN (1) | CN101517040B (ja) |
BR (1) | BRPI0717591B1 (ja) |
CA (1) | CA2663639C (ja) |
MX (1) | MX2009002395A (ja) |
RU (1) | RU2441054C2 (ja) |
WO (1) | WO2008038731A1 (ja) |
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JP2015151409A (ja) * | 2014-02-10 | 2015-08-24 | 株式会社テクネット | 油回収システム |
CN114672344B (zh) * | 2022-02-14 | 2023-10-03 | 浙江大学杭州国际科创中心 | 一种重油蒸汽裂解、产物分离回收小试装置及其使用方法 |
Citations (6)
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JPS5247007A (en) * | 1975-10-14 | 1977-04-14 | Kureha Chem Ind Co Ltd | Method and apparatus for preventing deposition of coke to vessels for thermal cracking of heavy hydrocarbons |
JPS5415444B2 (ja) | 1975-10-14 | 1979-06-14 | ||
JPS5715795B2 (ja) | 1977-02-04 | 1982-04-01 | ||
JPS59501068A (ja) * | 1982-06-14 | 1984-06-21 | ネステ・オ−・ワイ | 炭化水素油の熱分解方法 |
JPS6338076B2 (ja) | 1982-12-15 | 1988-07-28 | Kureha Chemical Ind Co Ltd | |
JPH0816450B2 (ja) | 1992-04-21 | 1996-02-21 | 川崎重工業株式会社 | 2サイクルエンジンの排気装置 |
Family Cites Families (9)
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NL104739C (ja) * | ||||
US2942043A (en) * | 1955-01-03 | 1960-06-21 | Hoechst Ag | Process for carrying out endothermic chemical reactions |
US3855339A (en) * | 1968-01-25 | 1974-12-17 | T Hosoi | Process for the thermal cracking of hydrocarbons |
DE2645649C2 (de) * | 1975-10-14 | 1982-09-02 | Chiyoda Chemical Engineering & Construction Co. Ltd., Yokohama, Kanagawa | Verfahren zum thermischen Cracken von schweren Kohlenwasserstoffen |
JPS5420006A (en) * | 1977-07-15 | 1979-02-15 | Yurika Kogyo Kk | Method of preventing foaming of heavy oil |
US4242196A (en) * | 1978-10-27 | 1980-12-30 | Kureha Kagaku Kogyo Kabushiki Kaisha | Mass production system of highly aromatic petroleum pitch |
EP0027692B1 (en) * | 1979-10-18 | 1984-05-30 | Imperial Chemical Industries Plc | A process and reactor for the pyrolysis of a hydrocarbon feedstock |
CN1031199C (zh) * | 1992-06-20 | 1996-03-06 | 彭培安 | 用废塑料生产燃料的方法及其装置 |
JP3415227B2 (ja) | 1993-10-28 | 2003-06-09 | 敏夫 淡路 | 有害物除去装置 |
-
2006
- 2006-09-28 JP JP2006264139A patent/JP4951302B2/ja active Active
-
2007
- 2007-09-27 WO PCT/JP2007/068853 patent/WO2008038731A1/ja active Search and Examination
- 2007-09-27 US US12/440,424 patent/US8262903B2/en not_active Expired - Fee Related
- 2007-09-27 EP EP07828599.6A patent/EP2072603A4/en not_active Withdrawn
- 2007-09-27 CA CA2663639A patent/CA2663639C/en active Active
- 2007-09-27 RU RU2009109849/04A patent/RU2441054C2/ru not_active IP Right Cessation
- 2007-09-27 CN CN2007800346313A patent/CN101517040B/zh not_active Expired - Fee Related
- 2007-09-27 MX MX2009002395A patent/MX2009002395A/es active IP Right Grant
- 2007-09-27 BR BRPI0717591A patent/BRPI0717591B1/pt not_active IP Right Cessation
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5247007A (en) * | 1975-10-14 | 1977-04-14 | Kureha Chem Ind Co Ltd | Method and apparatus for preventing deposition of coke to vessels for thermal cracking of heavy hydrocarbons |
JPS5415444B2 (ja) | 1975-10-14 | 1979-06-14 | ||
JPS5715795B2 (ja) | 1977-02-04 | 1982-04-01 | ||
JPS59501068A (ja) * | 1982-06-14 | 1984-06-21 | ネステ・オ−・ワイ | 炭化水素油の熱分解方法 |
JPS6338076B2 (ja) | 1982-12-15 | 1988-07-28 | Kureha Chemical Ind Co Ltd | |
JPH0816450B2 (ja) | 1992-04-21 | 1996-02-21 | 川崎重工業株式会社 | 2サイクルエンジンの排気装置 |
Non-Patent Citations (1)
Title |
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See also references of EP2072603A4 * |
Also Published As
Publication number | Publication date |
---|---|
BRPI0717591B1 (pt) | 2017-01-17 |
CA2663639C (en) | 2013-10-29 |
JP2008081629A (ja) | 2008-04-10 |
RU2009109849A (ru) | 2010-09-27 |
CA2663639A1 (en) | 2008-04-03 |
MX2009002395A (es) | 2009-05-15 |
CN101517040A (zh) | 2009-08-26 |
JP4951302B2 (ja) | 2012-06-13 |
US20100000909A1 (en) | 2010-01-07 |
CN101517040B (zh) | 2013-02-06 |
EP2072603A4 (en) | 2014-03-12 |
BRPI0717591A2 (pt) | 2013-10-29 |
US8262903B2 (en) | 2012-09-11 |
EP2072603A1 (en) | 2009-06-24 |
RU2441054C2 (ru) | 2012-01-27 |
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