CN113058332B - Method and device for removing coke powder in delayed coking fractionating tower - Google Patents
Method and device for removing coke powder in delayed coking fractionating tower Download PDFInfo
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- CN113058332B CN113058332B CN202110227141.7A CN202110227141A CN113058332B CN 113058332 B CN113058332 B CN 113058332B CN 202110227141 A CN202110227141 A CN 202110227141A CN 113058332 B CN113058332 B CN 113058332B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
- B01D45/08—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by impingement against baffle separators
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
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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
- C10G7/00—Distillation of hydrocarbon oils
Abstract
The invention provides a method and a device for removing coke powder in a delayed coking fractionating tower, which are characterized in that a heat exchange washing tank is arranged before oil gas enters the fractionating tower after quenching, a baffle plate demister, a cyclone and a partition plate are arranged in the fractionating tower, the reaction oil gas is subjected to heat exchange, washing, gas-liquid separation, liquid removal and decoking and other process treatments, most coke powder in the oil gas is washed to circulating oil, and thus the coke powder content of the fractionated oil gas is reduced. The circulating oil containing coke powder sinks from the lower outlet of the cyclone and fully sinks to the circulating oil at the bottom of the fractionating tower, after coke powder is removed from one part of the circulating oil at the bottom of the fractionating tower through a filter, the circulating oil respectively flows to the washing circulating oil distributor and the fractionating tower, and the other part of the circulating oil flows to the heating furnace and enters the circulation again. The invention can effectively reduce the content of coke powder in the fractionated oil gas, thereby improving the product quality of the delayed coking device, prolonging the operation period of the delayed coking device and downstream devices and saving the operation cost.
Description
Technical Field
The invention relates to a delayed coking technology in the field of petroleum refining, in particular to a method and a device for removing coke powder in a delayed coking fractionating tower, and more particularly, the device is used for carrying out cooling heat exchange, washing decoking, gas-liquid separation, liquid removal decoking and other process treatments on oil gas after quenching, and washing most of coke powder in the oil gas at the top of a tower to circulating oil at the bottom of the fractionating tower, thereby reducing the coke powder content of a delayed coking product.
Background
In recent years, because crude oil gradually tends to be inferior and heavy, and delayed coking has become one of the main processes for processing heavy oil in current oil refineries due to the advantages of strong raw material adaptability, obvious economic benefit and the like. The conventional delayed coking process comprises the following steps: the coking raw material enters a fractionating tower after being preheated by a convection section of a heating furnace, the heat exchange is carried out between the lower part of the fractionating tower and high-temperature coking oil gas from a coke tower, the bottom oil of the fractionating tower is pumped out and then enters a radiation section of the heating furnace, the heating is carried out until the coking temperature reaches the coking temperature, the coking reaction is carried out in the coke tower, the generated coke is left in the coke tower, the generated high-temperature oil gas enters the fractionating tower from the top of the coke tower to separate out coking rich gas, coking gasoline, coking diesel oil and coking wax oil, and part of reflux generated in the fractionating process is mixed with the coking raw material and then enters the circulation again. As a continuous, batch process, there are generally at least two coke drums, one of which is on-line while the other is performing the associated coke removal, and the two drums are alternately performing coke removal and coke removal.
In the conventional delayed coking process, a certain amount of coke powder is carried by coking rich gas and liquid products, and the safety and stability of processes such as downstream hydrogenation, acidic water treatment, catalysis and the like are seriously influenced. This is because the oil and gas from the coke drum going to the fractionation tower carries a significant amount of coke fines and enters the downflow product during the fractionation process. Optimizing the operating conditions in the production process is the most basic method for relieving the coke powder carrying, such as properly increasing the temperatures of the bottom of the fractionating tower and the outlet of the heating furnace, adopting high circulation ratio operation and the like. Reduce through optimizing operating condition and carry although easy operation, the desorption coke breeze effect is limited, can not thoroughly solve the problem that coking oil and contain the problem that sulphur sewage coke breeze carried, still need further through the coke breeze that technical transformation desorption coking oil and contain and carry in the sulphur sewage to reduce the influence to delay coking device and low reaches device and product.
Chinese utility model patent (CN 208762454U) discloses a device that slows down coking of coke tower top export oil gas pipeline, through set up into tower rapid cooling oil pipeline in vertical big oil gas pipeline, the interval sets up a plurality of shower nozzles on the outer fringe face of income tower rapid cooling oil pipeline, shower nozzle spun liquid drop contour line covers in the coke tower oil gas pipeline and the crossing looks of coke tower and passes through the face below region mutually, spray range covers this regional coke tower oil gas pipeline entry, with oil gas contact, cooling and washing, can slow down the coking of top of the tower oil gas export pipeline, the extension delays coker's start-up cycle etc. nevertheless because pipeline contact distance is short, and a large amount of atomized oil drips and high temperature oil gas contact back, can not play the decoking effect because of the endothermic gasification.
The Chinese patent of invention (CN 104046386B) discloses a delayed coking process method, which comprises the following steps: high-temperature oil gas from the top of the coke tower enters a cyclone separator in a tangential mode, and washing oil is injected into the top of the cyclone separator; the top oil gas of the cyclone separator is sent to a fractionating tower to separate coking products, bottom oil of the cyclone separator is separated into a material flow containing more coke powder and a material flow containing less coke powder through gravity or cyclone sedimentation, the material flow containing more coke powder is mixed with the material flow at the outlet of the heating furnace and then enters a coke tower to react, and the material flow containing less coke powder or mixed oil consisting of the material flow containing less coke powder and coking distillate oil is used as washing oil of the cyclone separator. The method and the device can improve the quality of the coking product and reduce the influence of coke powder on coking and downstream processes, but because high-temperature oil gas and washing oil at the top of the tower enter the cyclone separator together, the washing effect is poor, a buffer space is lacked, the requirement on the processing speed is high, and after a large amount of atomized oil drops contact the high-temperature oil gas, the decoking effect cannot be achieved due to heat absorption and gasification.
Therefore, it is necessary to design a method and a device for removing coke powder in a delayed coking fractionating tower, and simultaneously, the heat exchange washing, baffling demisting, cyclone decoking and other processes are adopted to fully reduce the coke powder content of the fractionated oil gas, thereby improving the product quality of the delayed coking device, prolonging the operation period of the delayed coking device and downstream devices and saving the operation cost.
Disclosure of Invention
The invention provides a method and a device for removing coke powder in a delayed coking fractionating tower, which can effectively reduce the coke powder content of the fractionated oil gas, thereby improving the product quality of the delayed coking device and prolonging the operation period of the delayed coking device and downstream devices.
One of the purposes of the invention is to provide a method for removing coke powder in a delayed coking fractionating tower, which comprises the following steps:
most coke powder in the quenched oil gas 10 is washed into circulating oil 7 at the bottom of a fractionating tower by carrying out cooling heat exchange, washing decoking, gas-liquid separation, liquid removal decoking and other process treatments on the quenched oil gas 10, so that the coke powder content of the fractionated oil gas is reduced. The method specifically comprises the following steps:
(a) After quenching, the oil gas 10 enters a heat exchange washing tank F, contacts with the atomized heat exchange wax oil 19 sprayed by the heat exchange wax oil distributor G for heat exchange, is subjected to opposite washing with the atomized washing circulating oil 17 sprayed by the washing circulating oil distributor H, and then flows to the lower part of the fractionating tower A. In the heat exchange process, the heat exchange wax oil 19 absorbs heat and is gasified, the oil gas releases heat and is cooled, and heavy oil components in the oil gas are condensed; the heat exchange wax oil 19 is divided for the wax oil 5 distilled from the fractionating tower, and the feeding flow of the heat exchange wax oil 19 is adjusted by a thermometer N through an automatic adjusting valve R3 according to the temperature of the washed oil gas 20. In the washing process, the foam coke carried by the oil gas is broken, and the coke powder is fully washed into a liquid phase; the feeding flow of the washing circulating oil 17 is adjusted by a flowmeter M through an automatic adjusting valve R2 according to the flow of the washing circulating oil;
(b) And (b) descending the oil gas 20 washed in the step (a) to pass through the left part of a baffle plate demister I at the bottom of the fractionating tower A to primarily remove a liquid phase and a solid phase in the oil gas, then ascending the oil gas to pass through the right part of the baffle plate demister I to secondarily remove coke and liquid and flow to a cyclone J, accumulating mist foam consisting of the liquid phase and the solid phase in the oil gas on the surface of the corrugated plate to form liquid drops, and finally separating the liquid drops to the circulating oil 7 at the bottom of the fractionating tower under the action of gravity. The liquid level height of the washing circulating oil 7 is indirectly controlled by adjusting the feeding flow through an automatic regulating valve R1 controlled by a liquid level meter S;
(c) The oil gas after the preliminary gas-liquid separation in the step (b) enters a cyclone J from a side port of the cyclone J, liquid phase and solid phase in the oil gas are thoroughly removed, under the action of strong centrifugal cyclone, clean oil gas rises and flows out from an upper outlet of the cyclone J, fractionation is carried out in a fractionating tower A, and an oil phase containing coke powder sinks and fully sinks to circulating oil 7 at the bottom of the fractionating tower from a lower outlet of the cyclone J;
(d) And (c) removing coke powder from one part of the circulating oil 7 at the bottom of the fractionating tower in the step (c) through a filter L, respectively flowing to a washing circulating oil distributor H and the fractionating tower A, and flowing the other part of the circulating oil to a heating furnace B for recycling.
In a preferred embodiment, the method further comprises the steps of: in step (a), the temperature of the oil gas after washing is 370-400 ℃.
In another preferred embodiment, in step (d), the height of the liquid level of the bottom circulating oil 7 of the fractionating tower is not less than 105% of the height from the bottom outlet of the separating tower A to the lower outlet of the cyclone J and not more than 85% of the height from the bottom outlet of the separating tower A to the lower end face of the baffle demister I.
Another object of the present invention is to provide a device for removing coke powder in a delayed coking fractionator, which comprises:
and the heat exchange washing tank F is internally provided with a heat exchange wax oil distributor G and a washing circulating oil distributor H and is used for heat exchange washing of the quenched oil gas 10. In the heat exchange washing process, the mass transfer is fully mixed, and the coke powder and heavy oil components in the oil gas 10 after quenching are washed to a liquid phase;
and the baffle plate demister I is used for preliminarily separating liquid phase and solid phase in the oil gas. Liquid phase and solid phase mist in the oil gas is accumulated on the surface of the corrugated plate to form liquid drops, and is finally separated to the circulating oil 7 at the bottom of the fractionating tower under the action of gravity;
and the cyclone J is used for further decoking and liquid removing. Because the centrifugal force borne by each phase is different, the oil gas rises and flows out from the upper outlet of the cyclone J, and is fractionated in the fractionating tower A, and the circulating oil containing coke powder sinks and fully sinks to the circulating oil 7 at the bottom of the fractionating tower from the lower outlet of the cyclone J;
and the partition plate K is used for separating and removing solid phase and liquid phase parts in the washed oil gas 20 from the fractionating tower A, and enabling the washed oil gas 20 to downwards pass through the baffle plate demister I, so that the oil gas for preliminarily separating the liquid phase and the solid phase enters from an inlet at the side edge of the cyclone J.
Heat transfer washing jar F set up after the quenching before oil gas 10 advances fractionating tower A, inside from the top down sets gradually heat transfer wax oil distributor G and washing cycle oil distributor H, baffling board defroster I sets up in fractionating tower A column base, the even array of swirler J is installed on baffle K, export passes baffling board defroster I under the swirler J and stretches into in the bottom cycle oil 7 of fractionating tower, the export passes baffle K on the swirler J, and set up the bubble cap in order to prevent the backward flow in the exit, swirler J side import is located baffle K downside, swirler J conic section bottom links to each other with baffling board defroster I top, horizontal baffle K height from the left to the right prevents the liquid gathering, vertical installation of vertical baffle K, vertical left side baffle K corresponds the sheet welding with baffling board defroster I and prevents to wash back oil gas 20 direct flow to swirler J.
In a preferred embodiment, the baffle demister I consists of a ridge baffle with a specific surface area of 200-350m 2 /m 3 The thickness of the demister is 0.007 to 0.014 of the height of the fractionating tower A.
In another preferred embodiment, the height of the lower outlet of the cyclone J from the outlet at the bottom of the fractionating tower A is 0.015-0.02 mm, and the height of the upper outlet penetrating the partition plate K is 180-230mm.
In another preferred embodiment, the angle between the transverse part of the partition K and the horizontal direction is 1-5 degrees, the distance between the longitudinal left partition K and the inlet of the washed oil gas 20 of the fractionating tower A is 0.08-0.12 of the diameter of the fractionating tower A, and the distance between the longitudinal right partition K and the inlet of the washed oil gas 20 of the fractionating tower A is 0.75-0.85 of the diameter of the fractionating tower A.
Has the beneficial effects that:
the method and the device have the main advantages that:
(1) The processes of heat exchange, washing, baffling demisting, centrifugal separation and the like of the invention realize the mixed mass transfer of the quenched oil gas and the washing circulating oil and promote the enrichment of coke powder and heavy oil components in the oil gas to an oil phase. Meanwhile, the ejection directions of the heat exchange wax oil distributor and the washing circulating oil distributor are opposite to the flowing direction of the oil gas, the generated inverse mixing action effectively reduces the gas velocity of the oil gas, strengthens the mixed mass transfer, and is beneficial to the full heat exchange and washing of the oil gas; the oil gas passes through the baffle plate demister from top to bottom and from bottom to top, liquid phase and solid phase carried in the oil gas are removed preliminarily, the oil gas is further centrifugally separated through the cyclone, the oil gas is fully subjected to liquid and coke removal, and the oil gas is fractionated after flowing out from the upper outlet of the cyclone, so that secondary entrainment is obviously reduced compared with the condition of only adopting a centrifugal separation device.
(2) Most of the devices for removing coke powder in the delayed coking fractionating tower are arranged in the fractionating tower, the structure is compact, and the occupied area of equipment is hardly increased. In addition, the oil phase for oil-gas heat exchange washing enters circulation again after being removed, and washing circulating oil is part of circulating oil at the bottom of the fractionating tower, is subjected to decoking through a filter and then is divided, so that the method has good economic benefit.
(3) The method and the device of the invention improve the operation period of the delayed coking device, reduce the content of coke powder in the delayed coking product, and are suitable for being widely popularized in the petrochemical industry.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification to further illustrate the invention and not limit the invention.
FIG. 1 is a schematic process flow diagram of a method and apparatus for reducing the coke powder content of delayed coking products according to a preferred embodiment of the present invention.
FIG. 2 is a schematic cross-sectional view of the bottom internals of a fractionation column according to a preferred embodiment of the present invention.
FIG. 3 is an enlarged view of a portion of FIG. 2, illustrating the connection of the left longitudinal partition to the baffle mist eliminator in accordance with a preferred embodiment of the present invention.
Wherein the reference characters denote the following devices and internals, respectively:
a: a fractionating column;
b: heating furnace;
c: a three-way plug valve;
d1 to D6: a shut-off valve;
e1, E2: a coking drum;
f: a heat exchange washing tank;
g: a heat exchange wax oil distributor;
h: a washing cycle oil distributor;
i: a baffle demister;
j: a swirler;
k: a partition plate;
l: a filter;
m: a flow meter;
n: a thermometer;
o: an air cooler;
p: a storage tank;
q: a heat exchanger;
r1 to R3: an automatic regulating valve;
s: a liquid level meter;
the numbers of the reference symbols represent the following streams, respectively:
1: coking the feedstock;
2: enriching gas;
3: gasoline;
4: diesel oil;
5: wax oil;
6: sulfur-containing sewage;
7: fractionating tower bottom circulating oil;
8: a coking oil;
9: reacting oil gas;
10: quenching the oil gas;
11: quenching oil;
12: returning wax oil;
13: refluxing the diesel oil;
14: refluxing gasoline;
15: fractionating the oil gas at the top of the tower;
16: wax oil is refluxed downwards;
17: washing the circulating oil;
18: circulating oil;
19: heat exchange wax oil;
20: and (5) washing the oil gas.
Detailed Description
In order to make the technical problems, technical solutions and advantageous effects solved by the present invention more clearly apparent, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and do not limit the invention.
After extensive and intensive research, the inventor of the application finds that the defects of poor decoking effect, secondary entrainment and the like in the existing decoking process can be effectively overcome through processes such as contact heat exchange, opposite flushing washing, baffling demisting, centrifugal separation and the like; meanwhile, most devices are arranged in the fractionating tower, so that the structure is compact, and the floor area of equipment is hardly increased; in addition, the oil phase for oil-gas heat exchange washing enters circulation again after being removed, and washing circulating oil is part of circulating oil at the bottom of the fractionating tower, is subjected to decoking through a filter and then is divided, so that the method has good economic benefit. The present invention has been completed based on the above conception and finding.
FIG. 1 is a schematic process flow diagram of a method and apparatus for reducing the coke powder content of delayed coking products according to a preferred embodiment of the present invention. Two coke drums E1 and E2 of the delayed coker, coke drum E1 being in the green stage and coke drum E2 being in the decoking stage. Three-way stopcock valve C points to coke drum E1. The states of the shut-off valves D1 to D6 related to the two coke drums E1 and E2 are as follows: a feeding cut-off valve D1 at the bottom of the coke tower E1, an oil-gas cut-off valve D3 at the top of the coke tower and a quenching oil cut-off valve D5 are opened; and a feeding cut-off valve D2 at the bottom of the coke tower E2, an oil-gas cut-off valve D4 at the top of the coke tower and a quenching oil cut-off valve F6 are closed. The coking raw material 1 firstly exchanges heat with the side line of the fractionating tower through each heat exchanger Q, is heated and then enters the circulating oil 7 at the bottom of the fractionating tower. A part of circulating oil 7 at the bottom of the fractionating tower flows to a filter L for decoking, a part of the circulating oil is heated to above 500 ℃ by a heating furnace B, coking oil 8 enters a raw coke tower E1 through a three-way plug valve C, and a series of cracking and condensation reactions are carried out on the coking oil 8 in the coke tower E1 to generate gas, naphtha, diesel oil, wax oil, circulating oil components and coke. The coke remains in the coke drum and the reaction oil gas 9 carrying a quantity of coke breeze exits the top of the coke drum R1 and is cooled to below about 430 c by the quench oil 11 to terminate the cracking reaction.
After quenching, the oil gas 10 enters a heat exchange washing tank F, contacts with the atomized heat exchange wax oil 19 sprayed by the heat exchange wax oil distributor G for heat exchange, then is washed by opposite flushing with the atomized washing circulating oil 17 sprayed by the washing circulating oil distributor H, and then flows to the lower part of the fractionating tower A. In the heat exchange process, the heat exchange wax oil 19 absorbs heat and is gasified, the oil gas releases heat and is cooled, and heavy oil components in the oil gas are condensed; the heat exchange wax oil 19 is branched for the wax oil 5 distilled from the fractionating tower, and the feeding flow of the heat exchange wax oil 19 is adjusted by a thermometer N through an automatic adjusting valve R3 according to the temperature of the washed oil gas 20. In the washing process, the foam coke carried by the oil gas is broken, and the coke powder is fully washed into a liquid phase; the feed flow rate of the washing circulating oil 17 is adjusted by the flow meter M by the automatic adjusting valve R2 according to its own flow rate. After washing, the oil gas 20 descends to pass through the left part of a baffle plate demister I at the bottom of the fractionating tower A to primarily remove liquid phase and solid phase in the oil gas, then the oil gas ascends to pass through the right part of the baffle plate demister I to secondarily remove coke and liquid and then flows to a cyclone J, mist formed by the liquid phase and the solid phase in the oil gas is accumulated into liquid drops on the surface of a corrugated plate, and finally is separated to the circulating oil 7 at the bottom of the fractionating tower under the action of gravity. The liquid level height of the washing circulating oil 7 is indirectly controlled by adjusting the feeding flow through an automatic adjusting valve R1 controlled by a liquid level meter S. Oil gas after primary gas-liquid separation enters the cyclone J from a side port of the cyclone J, liquid phase and solid phase in the oil gas are thoroughly removed, under the action of strong centrifugal cyclone, clean oil gas rises and flows out from an upper outlet of the cyclone J, and is fractionated in the fractionating tower A, and oil phase containing coke powder sinks and fully sinks to circulating oil 7 at the bottom of the fractionating tower from a lower outlet of the cyclone J. After coke powder is removed from one part of the circulating oil 7 at the bottom of the fractionating tower through a filter L, the part of the circulating oil respectively flows to a washing circulating oil distributor H and the fractionating tower A, and the other part of the circulating oil flows to a heating furnace B and enters the circulation again.
FIG. 2 is a schematic cross-sectional view of the bottom internals of a fractionation column according to a preferred embodiment of the present invention. And the baffle plate demister I is used for preliminarily separating liquid phase and solid phase in the oil gas. Mist formed by liquid phase and solid phase in the oil gas is accumulated on the surface of the corrugated plate to form liquid drops, and is finally separated to the circulating oil 7 at the bottom of the fractionating tower under the action of gravity; and the swirler J is used for further decoking and liquid removing. Because the centrifugal force of each phase is different, the oil gas rises and flows out from the upper outlet of the cyclone J, and is fractionated in the fractionating tower A, and the circulating oil containing coke powder sinks and fully sinks to the circulating oil 7 at the bottom of the fractionating tower from the lower outlet of the cyclone J; and the partition plate K is used for separating and removing solid phase and liquid phase parts in the washed oil gas 20 from the fractionating tower A, and enabling the washed oil gas 20 to downwards pass through the baffle plate demister I, so that the oil gas for preliminarily separating the liquid phase and the solid phase enters from an inlet at the side edge of the cyclone J. Baffling board defroster I set up in fractionating tower A post section bottom, the even array of swirler J is installed on baffle K, export passes baffling board defroster I under the swirler J and stretches into in the bottom circulating oil 7 of fractionating tower, export passes baffle K on the swirler J, and set up the bubble cap in order to prevent the backward flow in the exit, swirler J side import is located baffle K downside, swirler J conic section bottom links to each other with baffling board defroster I goes up the top, horizontal baffle K height from the left to the right prevents the liquid gathering, vertical installation of vertical baffle K, vertical left baffle K corresponds the slab welding with baffling board defroster I in order to prevent to wash back oil gas 20 direct flow to swirler J, vertical left baffle is connected the schematic diagram with the baffling board defroster and is shown in fig. 3.
In a delayed coking device of a certain oil refinery, oil gas carries more coke powder to enter a fractionating tower, so that a large amount of coking is caused on a heat exchange plate of the fractionating tower, a heat exchanger is scaled and blocked, the pressure drop of a bed layer of a downstream gasoline hydrogenation device and the like is higher, and the product quality is lower. After the method and the device for removing the coke powder in the delayed coking fractionating tower are adopted by the refinery, the coking phenomenon of a heat exchange plate of the fractionating tower is obviously reduced, the coke powder content in products such as wax oil, diesel oil, gasoline and the like is obviously reduced, and a hydrogenation device for downstream products runs stably.
Claims (7)
1. A method for removing coke powder in a delayed coking fractionating tower comprises the following steps:
(a) After quenching, the oil gas enters a heat exchange washing tank, contacts with atomized heat exchange wax oil sprayed by a heat exchange wax oil distributor for heat exchange, then is washed by opposite flushing with atomized washing circulating oil sprayed by a washing circulating oil distributor, and then flows to the lower part of a fractionating tower;
(b) Descending the oil gas washed in the step (a) to pass through a left baffle plate demister at the bottom of the tower to primarily remove a liquid phase and a solid phase in the oil gas, then ascending to pass through a right baffle plate demister to perform secondary decoking and liquid removal, and then flowing to a cyclone;
(c) Introducing the oil gas subjected to the preliminary gas-liquid separation in the step (b) into a cyclone from a side port of the cyclone, thoroughly removing liquid phase and solid phase in the oil gas, under the action of strong centrifugal cyclone, allowing the static oil gas to ascend from an upper outlet of the cyclone and flow out and fractionate on the middle upper part of a fractionating tower, and allowing the circulating oil containing coke powder to sink from a lower outlet of the cyclone and fully settle to the bottom of the fractionating tower;
(d) And (c) removing coke powder from one part of the circulating oil at the bottom of the fractionating tower in the step (c) through a filter, respectively flowing the part of the circulating oil to a washing circulating oil distributor and the fractionating tower, and flowing the other part of the circulating oil to a heating furnace to enter the circulation again.
2. The method of claim 1, wherein in step (a), the post-wash hydrocarbon temperature is 390-410 ℃.
3. The method of claim 1, wherein in step (d), the liquid level of the fractionation column bottoms recycle oil is no less than 105% of the height from the separation column bottom outlet to the lower outlet of the cyclone and no more than 85% of the height from the separation column bottom outlet to the lower end face of the baffle mist eliminator.
4. An apparatus for removing coke fines from a delayed coking fractionator, the apparatus comprising:
the heat exchange washing tank is internally provided with a heat exchange wax oil distributor and a washing circulating oil distributor and is used for carrying out heat exchange washing on the quenched oil gas; in the heat exchange washing process, the mass transfer is fully mixed, and the coke powder and the heavy oil in the oil gas after quenching are washed to a liquid phase;
the baffle plate demister is used for preliminarily separating a liquid phase and a solid phase in oil gas; liquid phase and solid phase mist in the oil gas is accumulated on the surface of the corrugated plate to form liquid drops, and is finally separated to the circulating oil at the bottom of the fractionating tower under the action of gravity;
the cyclone is used for further decoking and liquid removing; because the centrifugal force of each phase is different, the oil gas rises and flows out from the upper outlet of the cyclone, and is fractionated in the fractionating tower, and the circulating oil containing coke powder sinks and fully sinks to the circulating oil at the bottom of the fractionating tower from the lower outlet of the cyclone;
the separator is used for separating and removing the solid phase and the liquid phase in the washed oil gas from the fractionating tower, and enabling the washed oil gas to downwards pass through the baffle plate demister so that the oil gas which is preliminarily separated into the liquid phase and the solid phase enters from the side inlet of the cyclone;
the heat exchange washing tank is arranged before oil gas enters the fractionating tower after quenching, a heat exchange wax oil distributor and a washing circulating oil distributor are sequentially arranged from top to bottom inside the fractionating tower, the baffle plate demister is arranged at the bottom of a column section of the fractionating tower, the cyclone is uniformly arranged on the partition plate in an array mode, a lower outlet of the cyclone penetrates through the baffle plate demister to extend into circulating oil at the bottom of the fractionating tower, an upper outlet of the cyclone penetrates through the partition plate, a bubble cap is arranged at an outlet to prevent backflow, a side inlet of the cyclone is located at the lower side of the partition plate, the bottom of the cone section of the cyclone is connected with the upper top surface of the baffle plate demister, the horizontal partition plate is high in the left and low in the right to prevent liquid aggregation, the longitudinal partition plate is vertically arranged, and the longitudinal left partition plate and the baffle plate demister correspond to a plate and are welded to prevent the washed oil gas from directly flowing to the cyclone.
5. The apparatus as claimed in claim 4, wherein the baffle demister is composed of a ridge baffle having a specific surface area of 200-350m 2 /m 3 The thickness of the demister is 0.007 to 0.014 of the height of the fractionating tower.
6. The apparatus of claim 4, wherein the height of the lower outlet of the cyclone from the bottom outlet of the fractionating tower is 0.015-0.02 mm, and the height of the upper outlet through the partition is 180-230mm.
7. The apparatus of claim 4 wherein the partition has a transverse portion at an angle of 1 to 5 degrees from horizontal, the longitudinal left partition being spaced from the washed hydrocarbon inlet of the fractionation tower by a distance of 0.08 to 0.12 of the diameter of the fractionation tower, and the longitudinal right partition being spaced from the washed hydrocarbon inlet of the fractionation tower by a distance of 0.75 to 0.85 of the diameter of the fractionation tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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| DD235660A1 (en) * | 1985-03-29 | 1986-05-14 | Grotewohl Boehlen Veb | PROCESS FOR STABILIZING COLD PRODUCTS IN DELAYED DECOMPOSITION |
| US6193849B1 (en) * | 1995-04-21 | 2001-02-27 | William Lockett, Jr. | Fractionator with liquid-vapor separation means |
| CN1212369C (en) * | 2001-10-30 | 2005-07-27 | 中国石油化工股份有限公司 | Delayed coking process with low circulation ratio |
| CN203462007U (en) * | 2013-09-23 | 2014-03-05 | 博英睿科(北京)科技有限公司 | Delayed coking device capable of periodically controlling coke towers and fractionating tower |
| CN104804764B (en) * | 2014-01-26 | 2017-04-05 | 中石化洛阳工程有限公司 | A kind of delayed coking method |
| CN108753358A (en) * | 2018-05-31 | 2018-11-06 | 上海华畅环保设备发展有限公司 | Dry gas eddy flow liquid separation-cyclone desulfuration-eddy flow control alkali integrating device and its implementation in hydrogenation plant |
| CN112048330B (en) * | 2020-09-01 | 2021-09-10 | 北京奥博斯工程技术有限公司 | Process and device for reducing coke powder of delayed coking fractionating tower |
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