WO2011071113A1 - 油水分離装置及び精製装置 - Google Patents
油水分離装置及び精製装置 Download PDFInfo
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- WO2011071113A1 WO2011071113A1 PCT/JP2010/072136 JP2010072136W WO2011071113A1 WO 2011071113 A1 WO2011071113 A1 WO 2011071113A1 JP 2010072136 W JP2010072136 W JP 2010072136W WO 2011071113 A1 WO2011071113 A1 WO 2011071113A1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
- B01D17/04—Breaking emulsions
- B01D17/045—Breaking emulsions with coalescers
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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
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
Definitions
- the present invention relates to an oil / water separation device and a purification device.
- the present invention claims priority based on Japanese Patent Application No. 2009-280602 filed in Japan on December 10, 2009, the contents of which are incorporated herein by reference.
- Patent Document 1 discloses an oil / water separator that separates oil and water from water mixed with oil.
- This oil / water separator uses a combination of a perforated plate provided substantially at right angles to the flow of water mixed with oil and a baffle plate block provided at the rear of the perforated plate to remove oil that has flowed to the surface of the sea or the like. Collect efficiently.
- Patent Document 2 an oil / water separator provided with a partition plate member that forms a collision part that causes the flow path to meander and change the direction while generating turbulent flow in the oil / water separation tank. Is disclosed. In this oil / water separator, when water mixed with oil passes through the collision site, turbulent flow is generated in the water, and the flow direction of the water is changed.
- Patent Document 3 has a problem that the tar and particle removal process is complicated, resulting in a large apparatus configuration.
- the present invention has been made in view of the above-described circumstances, and has the following objects. (1) Provided is an oil-water separator that can be applied to oil-mixed water containing an oil component having a higher viscosity than before. (2) An oil / water separator having a simpler oil component separation structure than that of the prior art is provided.
- an oil mixed water supply port and an oil mixed water supplied from the supply port in a horizontal direction (a direction perpendicular to the vertical direction.
- the direction perpendicular to the vertical direction is defined as the “horizontal direction” and is simply referred to as “horizontal direction” hereinafter).
- an oil / water separator comprising a floating oil recovery port provided at a midway position away from the beginning of a path and a sedimented oil recovery port provided at a lower portion of a flow path.
- the supply port is provided at the center of a hollow cylindrical body supported in an upright posture along the vertical direction, and the flow path extends from the supply port to the body.
- the floating oil recovery port provides an oil / water separator that is a region sandwiched between the bottomless cylindrical member and the trunk provided concentrically between the supply port and the trunk.
- an oil-water separator comprising a rectifying means for suppressing a drift component different from the mainstream component of the oil-mixed water from the supply port toward the body in the second aspect.
- the partition member that divides the flow path into the divided flow paths that are multistage in the vertical direction and whose end ends lower than the start end is provided on the outlet side of the flow path.
- An oil / water separation device is provided.
- a fifth invention according to the present invention is a purifying apparatus for purifying by removing at least oil from the gas to be purified, and at least the oil in the gas to be purified is separated from the gas to be purified by spraying water.
- a refining apparatus comprising a spray tower and an oil / water separator according to any one of the first to fourth inventions for separating oil from oil mixed water discharged from the spray tower.
- a mist separator that separates oil from the gas to be purified again may be provided at the rear stage of the spray tower.
- the gas to be purified may be a gasification gas generated using lignite as a raw material.
- the oil component contained in the oil-mixed water that has a specific gravity greater than water settles and is collected at the lower part of the flow path. Smaller ones rise and are collected at the top of the channel. That is, in this invention, an oil component is isolate
- grains in a separation zone It is a graph which shows the calculation result of. It is a characteristic view which shows the sedimentation and the floating locus
- the purification apparatus A includes a spray tower 1, a mist separator 2, a tar decanter 3 (oil / water separator), a buffer tank 4, a tar tank 5, pumps 6 to 8, and a cooler 9. It is composed of This purification apparatus A is an apparatus for purifying gasification gas X1 (purification target gas) supplied from the outside.
- gasification gas X1 purification target gas
- gasified gas is known as a combustible gas obtained by steam reforming biomass or coal, and is useful as a fuel and a constituent raw material.
- the gasification gas X1 in the present embodiment is obtained by steam reforming a relatively poor brown coal among coal, and has extremely high viscosity tar (oil), sludge as solid particles other than oil, and Including water vapor.
- the spray tower 1 sprays cooling water X2 on the gasification gas X1 to be treated to cool the gasification gas X1, and separates and removes sludge contained in the gasification gas X1 from the gasification gas X1.
- the spray tower 1 cools, for example, a gasified gas X1 at 400 ° C. to about 75 ° C., and this cooling condenses oil (mainly tar components) contained in the gasified gas X1.
- the spray tower 1 supplies the treated gasified gas X 3 to the mist separator 2, while discharging the oil mixed water X 4 composed of water, tar particles and sludge to the tar decanter 3.
- the mist separator 2 is provided as a supplement to the spray tower 1 and sprays the separated water X5 onto the treated gasified gas X3 supplied from the spray tower 1 as finer water droplets than the cooling water X2.
- the mist-like unnecessary oil components and sludge that cannot be sufficiently separated and removed by the tower 1 are removed.
- the mist separator 2 outputs the treated gasification gas to the outside as a purified gas X6, while discharging the oil mixed water X7 composed of water, tar particles and sludge to the tar decanter 3.
- the tar decanter 3 is the most characteristic component in the refining apparatus A, and tar particles and sludge contained in the oil mixed water X4 supplied from the spray tower 1 and the oil mixed water X7 supplied from the mist separator 2 are obtained.
- the specific gravity is separated into particles that are heavier than water and the specific gravity is lighter than water. That is, the tar decanter 3 separates various particles contained in water into particles having a specific gravity heavier than water and particles lighter than water by utilizing the specific gravity and particle size.
- the tar decanter 3 discharges particles having a specific gravity heavier than water from the bottom as precipitated tar X8, and discharges particles having a specific gravity lighter than water from the top as floating tar X9, so that the precipitated tar X8 and the floating tar X9 are separated.
- the treated water X10 is discharged from the top.
- the buffer tank 4 is a storage tank for temporarily storing the treated water X10 supplied from the upper part of the tar decanter 3 and a supply source of the cooling water X2 and the separated water X5.
- the treated water X 10 is sequentially supplied from the tar decanter 3, while a part of the treated water X 10 is pumped out by the pumps 7 and 8, so surplus water is generated.
- the buffer tank 4 drains such excess water to the outside.
- the tar tank 5 is a storage tank for temporarily storing the precipitated tar X8 supplied from the lower part of the tar decanter 3.
- the pump 6 is provided at an intermediate portion of the pipe connecting the lower portion of the tar decanter 3 and the tar tank 5, and discharges the precipitated tar X 8 accumulated in the lower portion of the tar decanter 3 and supplies it to the tar tank 5.
- the pump 7 is provided in the middle part of the pipe connecting the buffer tank 4 and the mist separator 2, pumps up the treated water X10 from the buffer tank 4, and supplies it to the mist separator 2 as separated water X5.
- the pump 8 is provided at an intermediate portion of the pipe connecting the buffer tank 4 and the spray tower 1, and pumps the treated water X 10 from the buffer tank 4 and supplies it to the spray tower 1.
- the cooler 9 is provided between the pump 8 and the spray tower 1 in a pipe connecting the buffer tank 4 and the spray tower 1, and cools the treated water X10 supplied from the pump 8 by heat exchange with an external heat medium.
- the cooling water X2 is supplied to the spray tower 1.
- the tar decanter 3 (oil / water separator) which is the most characteristic component in the refining apparatus A will be described with reference to FIG.
- the tar decanter 3 includes an apparatus body 3a, a supply pipe 3b (supply port), a center well 3c, a recovery baffle 3d, an upper storage part 3e, and a lower storage part 3f.
- the apparatus body 3a is a hollow cylindrical body fixed in an upright posture along the vertical direction, and an upper part is released, while a lower storage part 3f is connected to the lower part. That is, the device body 3a is configured as a substantially cylindrical container integrated with the lower storage portion 3f.
- the supply pipe 3b is a pipe provided concentrically with respect to the axial center (center) of the apparatus body 3a, and supplies oil mixed water X4 and X7 downward from the lower end.
- the center well 3c is a cylindrical member concentric with the apparatus body 3a and the supply pipe 3b in an upright posture along the vertical direction and provided between the supply pipe 3b and the apparatus body 3a. As shown in the drawing, the position of the tip (lower edge) of the center well 3c is set lower than the position of the tip (lower edge) of the supply pipe 3b by a predetermined dimension.
- the collection baffle 3d is a cylindrical member provided concentrically with the apparatus body 3a and the supply pipe 3b between the center well 3c and the apparatus body 3a in an upright posture along the vertical direction in the same manner as the center well 3c. is there. As shown in the figure, the position of the front end (lower edge) of the recovery baffle 3d is set higher than the position of the front end (lower edge) of the center well 3c by a predetermined dimension.
- the disc-shaped region located below the center well 3c and having the outer periphery directly below the collection baffle 3d tar particles and sludge contained in the oil mixed water X4 and X7 flow in the horizontal direction.
- This is a separation zone R that is separated based on the specific gravity while reaching the position directly below the recovery baffle 3d.
- the opening region between the lower edge of the center well 3c and the lower edge of the recovery baffle 3d is a floating oil recovery port F in the tar decanter 3 (oil / water separator), and the lower edge of the recovery baffle 3d and the device body 3a.
- the opening area between the two is mainly a water recovery port M from which treated water is selectively recovered.
- the upper storage portion 3e is a ring-shaped portion that surrounds the apparatus body 3a around the upper outer periphery of the apparatus body 3a, and is located above the tar decanter 3 and supplies the floating tar X9 to the buffer tank 4.
- the upper edge of the apparatus body 3a is set lower than the upper edge of the center well 3c, the upper edge of the collection baffle 3d, and the upper edge of the upper reservoir 3e as shown in the figure.
- the water level (draft) in the tar decanter 3 is the upper edge of the apparatus body 3a as shown by a one-dot chain line in FIG.
- the treated water X10 overflowing from the upper edge of the apparatus body 3a is collected in the upper reservoir 3e and then supplied from the reservoir 3e to the buffer tank 4.
- the lower reservoir 3 f is formed in an inverted conical shape as a whole as shown in the figure, and is located at the lower part of the tar decanter 3. Oil components and sludge separated in the separation zone R and having a specific gravity heavier than water are deposited in the lower reservoir 3f.
- a pipe for supplying the precipitated tar X8 to the tar tank 5 is connected to the center of the lower portion of the lower storage portion 3f (lower portion of the tar decanter 3).
- the angle of repose ⁇ in the shape of the lower reservoir 3f is set to 45 °, for example, so that oil components and sludge having a specific gravity heavier than water are effectively discharged.
- the upper end opening region of the lower reservoir 3f (that is, the lower end opening region of the apparatus body 3a) is a sedimented oil recovery port T in the tar decanter 3 (oil / water separator).
- tar (oil), sludge (solid content), and water vapor (water) are removed from the gasification gas X1 to be purified by the action of the cooling water X2 in the spray tower 1, and subsequently the mist separator. 2, tar, sludge and water vapor are removed by the action of separated water X5. That is, the gasification gas X1 is purified in two stages by the spray tower 1 and the mist separator 2, and as a result, purified gas X6 purified to a higher purity than that in the normal one-stage purification is produced.
- the oil-mixed water X4, X7 generated by the respective refining processes in the spray tower 1 and the mist separator 2 is collected in the tar decanter 3 and sent as a gentle flow into the tar decanter 3 through the supply pipe 3b. Since the oil mixed water X4 and X7 flowing out downward from the tip of the supply pipe 3b as a gentle flow is drained from the tar decanter 3 from the upper edge of the apparatus body 3a as described above, The flow direction changes to the horizontal direction and flows toward the apparatus body 3a.
- the separation zone R described above is a flow field in which the horizontal flow component of such oil mixed water X4, X7 becomes the mainstream component.
- tar particles and sludge contained in the oil-mixed water X4 and X7 flowing gently from the center well 3c toward the apparatus body 3a have their own specific gravity, particle diameter, and moving speed (terminal speed) with respect to water.
- the horizontal distance D from the lower edge of the center well 3c to the lower edge of the collection baffle 3d and the vertical distance (distance along the vertical direction) H of the lower edge of the collection baffle 3d with respect to the lower edge of the center well 3c are the floating tar.
- the horizontal distance D and the vertical distance H are based on the end velocity V of the tar particles given by the Stokes equation, the Allen equation or the Newton equation, the particle size distribution and the specific gravity of the tar particles, etc., depending on the Reynolds number of the tar particles.
- Optimal setting is such that most of the tar particles having a specific gravity smaller than that of water flow into the floating oil recovery port F.
- tar contained in lignite is formed from naphthalene oil, carbol oil, washing oil, anthracene oil, and pitch as described in well-known literature.
- naphthalene oil has a specific gravity of 0.98 and a specific gravity smaller than that of water
- carboru oil, washing oil, anthracene oil and pitch have a specific gravity of 1 or more and a specific gravity larger than that of water. Therefore, naphthalene oil forms the above-mentioned floating tar X9
- carbol oil, washing oil, anthracene oil and pitch form precipitated tar X8.
- the horizontal distance D and the vertical distance H are set so that most of the naphthalene oil particles forming the floating tar X9 flow into the floating oil recovery port F.
- FIG. 4A to 4C are graphs showing the calculation results of the terminal velocity (floating velocity or sedimentation velocity) according to the particle size (oil droplet diameter) of each tar particle in the separation zone R.
- FIG. 4A shows the flying speed (terminal speed) according to the oil droplet diameter for naphthalene oil (floating oil) and particles having a specific gravity close to that of naphthalene oil (reference particles)
- FIG. 4B shows carboru oil (settling oil). )
- particles having a specific gravity close to carboru oil (reference particles) the sedimentation velocity (terminal velocity) according to the oil droplet diameter is shown, and FIG.
- FIG. 4C shows SS particles (sludge) and particles having a specific gravity close to SS particles (reference particles).
- the sedimentation velocity (end velocity) according to the particle diameter is shown. From any graph, it can be seen that the terminal velocity changes according to the particle diameter.
- the final speed (movement speed) of the tar particles and sludge in the separation zone R is an extremely important factor that determines whether the tar particles and sludge flow into the sedimented oil recovery port T or the water recovery port M.
- FIG. 5 is a characteristic diagram showing the sedimentation and levitation trajectories of the representative particle diameters of the tar particles.
- the floating trajectory is shown when the representative particle size is 200 ⁇ m and 300 ⁇ m, and for carboru oil (precipitated oil), when the representative particle size is 500 ⁇ m, SS particle (sludge) ) Shows the sedimentation trajectory when the representative particle size is 60 ⁇ m.
- These representative particle sizes are average particle sizes of tar particles and sludge (SS particles) contained in the oil mixed water X4 and X7.
- naphthalene oil floating oil
- the vertical position when reaching the collection baffle 3d differs greatly between the case where the representative particle size is 200 ⁇ m and the case where the representative particle size is 300 ⁇ m. Therefore, it is necessary to optimize the horizontal distance D and the vertical distance H in consideration of the particle size distribution of the naphthalene oil contained in the oil mixed water X4 and X7.
- the tar decanter 3 with a plurality of zones divided by the apparatus body 3a, the center well 3c and the recovery baffle 3d, a plurality of particles having different specific gravities are allowed to pass through the plurality of zones through the settling oil recovery port T or The water can be selectively and simultaneously recovered from the water recovery port M. Therefore, further separation of the floating oil can be easily performed. Furthermore, according to this refining apparatus A, since such a tar decanter 3 is employed, it is possible to purify oil-mixed water containing an oil component having a higher viscosity than before, and at a low cost.
- the flow components in the horizontal direction of the oil mixed waters X4 and X7 are the flow fields of the mainstream components, but the flow directions of the oil mixed waters X4 and X7 supplied from the supply pipe 3b. Is a direction from top to bottom, and therefore, the oil mixed water X4 and X7 flowing through the separation zone R locally includes a vertical flow component (a drift component) different from the main flow component.
- a drift component a vertical flow component
- tar decanters 3A to 3D according to modifications as shown in FIGS. 6A to 6D are conceivable.
- rectifying members 10A to 10D rectifying means for suppressing the drift component are provided below the center well 3c.
- the rectifying member 10A in the tar decanter 3A is a disk-shaped flat plate, and is provided in a horizontal posture below a predetermined distance from the lower edge of the center well 3c. Further, the axis of the rectifying member 10A coincides with the axis of the center well 3c. According to such a rectifying member 10A, as shown in the figure, the flow of the oil mixed water X4, X7 supplied from the supply pipe 3b is regulated by the rectifying member 10A and becomes a mainstream component.
- the rectifying member 10B in the tar decanter 3B is a disc-shaped punching metal, and is attached to the lower edge of the center well 3c in a horizontal posture.
- the axis of the rectifying member 10B coincides with the axis of the center well 3c. According to such a rectifying member 10B, as shown in the figure, the flow of the oil mixed water X4, X7 supplied from the supply pipe 3b is finely divided by the rectifying member 10B, so that the mainstream component increases.
- the rectifying member 10C in the tar decanter 3C is a conical member, with the apex facing upward at a lower position at a predetermined distance from the lower edge of the center well 3c, and the shaft core coincides with the shaft core of the center well 3c. It is provided as follows. According to such a rectifying member 10C, as shown in the figure, the flow of the oil-mixed water X4, X7 supplied from the supply pipe 3b is redirected by the conical surface of the rectifying member 10C to become a mainstream component.
- the rectifying member 10D in the tar decanter 3D is a turbine blade-shaped member (fixed blade) having a conical shape as a whole, with the apex directed upward at a lower position at a predetermined distance from the lower edge of the center well 3c, and
- the shaft core is provided in a posture that matches the shaft core of the center well 3c.
- a tar decanter 3F shown in FIG. 7 is conceivable as a modification for suppressing the above-described drift component.
- a partition member 11 for dividing the flow path into a plurality of stages in the vertical direction is provided on the outlet side (recovery baffle 3d side) in the flow path from the center well 3c to the recovery baffle 3d.
- the partition member 11 partitions the flow path into four stages in the vertical direction, and at a predetermined angle (for example, 45 °) so that the end (collection baffle 3d side) is lower than the start end (center well 3c side). It is provided in an inclined state.
- the outlet side of the flow path from the center well 3c to the recovery baffle 3d is arranged in the vertical direction and descends with a constant inclination from the inlet side (center well 3c side) to the outlet side. It is divided into four divided flow paths.
- the outlet side of the flow path from the center well 3c to the recovery baffle 3d is partitioned into four stages in the vertical direction, so that the vertical flow path width is limited and the drift component is suppressed. be able to.
- the four segmental channels are formed so as to descend at a constant inclination toward the outlet side, so that the channel length is substantially increased.
- the time (movement time) for moving tar particles and sludge from the center well 3c to the recovery baffle 3d becomes longer, and the floating oil is easily separated.
- the vertical width of each sorting channel formed by the partition member 11 is set so that tar particles and sludge do not adhere to the partition member 11 and block the sorting channel.
- drum 3a are arranged.
- the region between them is a channel through which the oil mixed water X4 and X7 flows, but the channel is not limited to this.
- a supply port is provided in a line along one side of a rectangular flow path in plan view, and a line-shaped upper storage portion (in parallel to the supply port at a position facing the line-shaped supply port ( A water recovery port) may be provided, and a rectangular region between the line-shaped supply port and the upper reservoir (water recovery port) may be used as the flow path.
- the gasification gas X1 is the gas to be purified, but the gas to be purified is not limited to this. Further, the treatment target of the tar decanter 3 is not limited to the oil mixed water X4 and X7 containing the tar particles and sludge separated from the gasification gas X1.
- the oil / water separator of the present invention a highly viscous oil can be separated from water. Moreover, since it is only necessary to circulate the oil-mixed water through the flow path, the configuration of the apparatus is simpler than that of the prior art, and thus cost reduction can be realized. Furthermore, according to the refining device of the present invention, it is possible to purify a gasification gas containing an oil component having a higher viscosity than before, and to reduce the cost for refining.
- a ... refining device 1 ... spray tower, 2 ... mist separator, 3 ... tar decanter, 3a ... device body, 3b ... supply pipe (supply port), 3c ... center well, 3d ... recovery baffle, 3e ... upper reservoir, 3f: Lower storage section, 4 ... Buffer tank, 5 ... Tar tank, 6, 7, 8 ... Pump, 9 ... Cooler, X1 ... Gasification gas (purification target gas), X2 ... Cooling water, X3 ... Treated gas Gas, X4, X7 ... oil mixed water, X5 ... separated water, X6 ... purified gas, X8 ... precipitation tar, X9 ... floating tar, X10 ... water, T ... precipitation oil recovery port, F ... floating oil recovery port, M ... Water recovery port,
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Abstract
Description
また、下記特許文献2には、油水分離槽内に、流路を蛇行させて長くするとともに水に乱流を発生させつつ方向を転換させる衝突部位を形成する仕切板部材を設けた油水分離装置が開示されている。この油水分離装置では、油が混合した水が上記衝突部位を通過する際に、水に乱流が発生し、かつ水の流下方向が転換される。そのため、水中の粒子どうしがぶつかり合って油粒子や水粒子の凝集が促進され、また油粒子が仕切板部材に付着しつつ粗大化し、この結果として油水が比重差により分離される。
さらに、下記特許文献3には、タール含有ガスの洗浄技術として、油スクラバを用いた重質タールの除去と、水スクラバを用いた軽質タールの除去と、サイクロンを用いた粒子成分の除去との組み合わせが開示されている。
このような背景から、例えば石炭(特に褐炭)を原料として改質・生成されたガス化ガスのように、極めて粘度の高いタール分(油分)と水分とを含む油混合水について、上記従来の油水分離装置を適用することは現実的に不可能である。よって、極めて粘度の高い油分を含む油混合水に適用し得る新たな油水分離装置の開発が切望されている。
また、特許文献3の洗浄技術では、タールや粒子の除去プロセスが複雑なので、装置構成が大型化するという問題がある。
(1)従来よりも粘度の高い油分を含む油混合水に適用し得る油水分離装置を提供する。
(2)油成分の分離構成が従来よりも簡単な油水分離装置を提供する。
また、本発明によれば、油混合水を流路に流通させるだけで良いので、装置の構成が従来よりも簡単であり、よって低コスト化を実現することができる。
さらに、本発明によれば、従来よりも粘度の高い油分を含むガス化ガスを精製することが可能であると共に精製に関するコストを低減することができる。
本実施形態に係る精製装置Aは、図1に示すように、スプレー塔1、ミストセパレータ2、タールデカンタ3(油水分離装置)、バッファタンク4、タールタンク5、ポンプ6~8及び冷却器9から構成されている。この精製装置Aは、外部から供給されたガス化ガスX1(精製対象ガス)を精製する装置である。
タールデカンタ3は、図2に示すように、装置胴体3a、供給管3b(供給口)、センターウエル3c、回収バッフル3d、上部貯留部3e及び下部貯留部3fから構成されている。
図3において符号Pで示す粒子は、分離ゾーンRにおける上記タール粒子及びスラッジの挙動を模式的に示している。
また、タールの比重を利用して浮上油と沈降油とを分離ゾーンRを通過させるだけで容易かつ同時に分離することができるので、油成分の分離に関する構成が従来よりも簡単であり、よって低コストである。しかも、タールデカンタ3に、装置胴体3a、センターウエル3c及び回収バッフル3dにより分かれた複数のゾーンを設けることにより、比重の異なる複数の粒子を、これら複数のゾーンを介して沈降油回収口Tまたは水回収口Mから選択的かつ同時に回収することができる。そのため、浮上油の更なる分別を容易に行なうことができる。
さらに、本精製装置Aによれば、このようなタールデカンタ3を採用するので、従来よりも粘度の高い油分を含む油混合水を精製することが可能であると共に低コストである。
(1)上述したように分離ゾーンRは、油混合水X4,X7の水平方向の流れ成分が主流成分の流場であるが、供給管3bから供給される油混合水X4,X7の流れ方向は上から下に向かう方向であり、よって分離ゾーンRを流れる油混合水X4,X7は上記主流成分とは異なる鉛直方向の流れ成分(偏流成分)を局所的に含む。しかし、上述した水平距離D及び垂直距離Hを設定(設計)する場合には、分離ゾーンRの流場の速度成分を上記主流成分のみとして設計せざるを得ないので、分離ゾーンRにおける偏流成分を極力抑制する必要がある。
Claims (12)
- 油混合水の供給口と、
供給口から供給された油混合水を水平方向の流れ成分を主流成分となるように流通させる流路と、
流路の上部かつ前記流路の始端から離間した途中位置に設けられた浮上油回収口と、
前記流路の下部に設けられた沈降油回収口と
を具備する油水分離装置。 - 前記供給口は、鉛直方向に沿って直立姿勢に支持された中空円筒状の胴体の中心に設けられ、
前記流路は、前記供給口から前記胴体までの部位であり、
前記浮上油回収口は、前記供給口と前記胴体との間に同心状に設けられた無底円筒材と前記胴体とによって挟まれた領域である
請求項1記載の油水分離装置。 - 前記供給口から前記胴体に向う油混合水の主流成分とは異なる偏流成分を抑制する整流手段を備える請求項2記載の油水分離装置。
- 鉛直方向に多段かつ始端よりも終端が下がる区分流路に流路を区画する区画部材を流路の出口側に備える請求項1~3のいずれか一項に記載の油水分離装置。
- 精製対象ガスから少なくとも油分を除去することにより精製する精製装置であって、
水を噴霧することにより精製対象ガス内の少なくとも油分を精製対象ガスから分離するスプレー塔と、
スプレー塔から排出される油混合水から油分を分離する請求項1~3のいずれか一項に記載の油水分離装置と
を具備する精製装置。 - 精製対象ガスから少なくとも油分を除去することにより精製する精製装置であって、
水を噴霧することにより精製対象ガス内の少なくとも油分を精製対象ガスから分離するスプレー塔と、
スプレー塔から排出される油混合水から油分を分離する請求項4に記載の油水分離装置と
を具備する精製装置。 - スプレー塔の後段に、精製対象ガスから油分を再度分離するミストセパレータを備える請求項5に記載の精製装置。
- スプレー塔の後段に、精製対象ガスから油分を再度分離するミストセパレータを備える請求項6に記載の精製装置。
- 精製対象ガスは褐炭を原料として生成されたガス化ガスである請求項5に記載の精製装置。
- 精製対象ガスは褐炭を原料として生成されたガス化ガスである請求項6に記載の精製装置。
- 精製対象ガスは褐炭を原料として生成されたガス化ガスである請求項7に記載の精製装置。
- 精製対象ガスは褐炭を原料として生成されたガス化ガスである請求項8に記載の精製装置。
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JP2011545243A JP5387692B2 (ja) | 2009-12-10 | 2010-12-09 | 油水分離装置及び精製装置 |
US13/514,480 US8864888B2 (en) | 2009-12-10 | 2010-12-09 | Oil-water separation device and refining device |
CN201080053782.5A CN102655920B (zh) | 2009-12-10 | 2010-12-09 | 油水分离装置和纯化装置 |
AU2010329034A AU2010329034B2 (en) | 2009-12-10 | 2010-12-09 | Oil-water separation device and refining device |
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JP (1) | JP5387692B2 (ja) |
CN (1) | CN102655920B (ja) |
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CN109513236A (zh) * | 2018-12-27 | 2019-03-26 | 中冶焦耐(大连)工程技术有限公司 | 一种用于脱酚洗涤泵前混合工艺的连洗分离塔 |
CN109647005A (zh) * | 2019-01-11 | 2019-04-19 | 中冶焦耐(大连)工程技术有限公司 | 一种脱酚洗涤泵前混合工艺及装置 |
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AU2010329034A1 (en) | 2012-07-12 |
JP5387692B2 (ja) | 2014-01-15 |
JPWO2011071113A1 (ja) | 2013-04-22 |
AU2010329034B2 (en) | 2014-01-23 |
US20120255900A1 (en) | 2012-10-11 |
CN102655920B (zh) | 2015-03-18 |
CN102655920A (zh) | 2012-09-05 |
US8864888B2 (en) | 2014-10-21 |
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