CN109868154B - Method for reducing heavy oil carrying of emptying tower of delayed coking device - Google Patents
Method for reducing heavy oil carrying of emptying tower of delayed coking device Download PDFInfo
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Abstract
The invention discloses a method for reducing heavy oil carrying in an emptying tower of a delayed coking device, wherein in a steam blowing and emptying stage of a coke tower, a cooling medium is injected into emptying gas to cool the emptying gas; the temperature of oil gas entering the emptying tower is reduced by adjusting the injection amount of the cooling medium; so as to reduce the gas velocity of the empty tower in the emptying tower; arranging a heater for emptying tower bottom oil, returning heavy sump oil at the bottom of a stock tower at the outlet of an emptying tower bottom pump to an inlet pipeline of the emptying tower after the heavy sump oil at the bottom of the emptying tower is heated by the heater, and maintaining the temperature of a liquid phase entering the emptying tower through the flow of a heating medium; to avoid bumping of the bottom of the tower caused by water in the liquid phase; a pressure control valve is arranged on a noncondensable gas outlet pipeline of a liquid separation tank at the top of the emptying tower, so that the pressure at the top of the emptying tower is increased when the coke tower blows steam and is emptied; so as to reduce the gas velocity of the empty tower in the emptying tower; and a washing baffle is arranged in the tower, and the heavy oil in the oil gas is further washed by high-temperature heavy oil. The invention can effectively reduce the air speed of the empty tower in the emptying tower, avoid the sudden boiling of the water at the bottom of the emptying tower, improve the washing effect of heavy oil, reduce the heavy oil carrying of the gas phase at the top of the emptying tower, prolong the operation period of a cooler at the top of the emptying tower and reduce the heavy oil content of the sewage at the top of the emptying tower by a combined means.
Description
Technical Field
The invention relates to a delayed coking technology in the field of petroleum refining, in particular to a method for reducing heavy oil carrying of an empty tower of a delayed coking device.
Background
The delayed coking process is an important inferior heavy oil processing technology, and as a continuous production and discontinuous operation process, generally, at least two coke drums are provided, when one coke drum is in on-line coke formation, the other coke drum performs coke removal related operation, and the two coke drums alternately perform coke formation and coke removal operation. The coke tower for decoking needs to be subjected to the steps of small steam blowing, large steam blowing, water supply and coke cooling, water drainage, opening of a coke tower top bottom cover, hydraulic coke cutting, closing of the coke tower top bottom cover, steam air removal, steam pressure testing, oil gas preheating, switching feeding and the like. The vent tower of the delayed coking device mainly treats gas discharged from the top of the decoking coke tower in the process from the beginning of the atmospheric steam blowing step to the ending of the steps of closing the vent isolating valve and opening the breather valve during water supply and coke cooling, and the discharged gas mainly contains gas, light dirty oil, heavy dirty oil and steam.
The process flow of the steam blowing and emptying process of the prior delayed coking unit is explained by combining with the attached figure 1.
The delayed coking device coke-forming coke tower A is in a coke-forming stage, the four-way valve K points to the coke-forming coke tower A, a side feeding block valve L1 of the coke tower A is opened, a side oil-throwing main valve M1 of the coke tower A is closed, a side bottom steam-blowing valve N1 of the coke tower A is closed, and a side bottom water-feeding valve O1 of the coke tower A is closed; the big oil-gas isolating valve P1 at the side of the coke tower A is opened, and the blowing and emptying isolating valve R1 at the side of the coke tower A is closed. The coking oil 1 from the coking heating furnace enters a raw coke tower A through a four-way valve K, a series of cracking and condensation reactions occur in the coke tower, the coke generated by the reactions is remained in the coke tower, the coking oil gas 2 produced by the reactions flows out from the top of the coke tower, and different fractions are separated from the coking oil gas through a large oil gas pipeline to a coking fractionation system after being cooled by quenching oil.
When the decoking coke tower B is in a large steam blowing and water supply coke cooling stage, a side feeding block valve L2 of the coke tower B is closed, an oil throwing main valve M2 of the coke tower B is opened, a large oil and gas block valve P2 of the coke tower B is closed, and a side steam blowing and emptying block valve R2 of the coke tower B is opened. When the decoking coke drum B is subjected to large steam blowing operation, the bottom steam blowing valve N2 on the side of the coke drum B is opened, and the water feeding valve O2 on the side of the coke drum B is closed; when the decoking coke drum B is subjected to the feed water cooling operation, the coke drum B side bottom blow valve N2 is closed and the coke drum B side bottom feed water valve O2 is opened.
In the process of large steam blowing and water supply of the decoking coke tower B, the generated high-temperature (150-420 ℃) vent gas 3 consisting of a large amount of steam and a small amount of oil gas enters the lower part of the vent tower C from the top of the decoking coke tower B, a heat exchange plate is arranged in the vent tower C, the vent gas is in the tower to contact with heavy dirty oil 6 entering from the top of the tower for heat exchange, heavy oil fractions in the oil gas are condensed and absorbed and fall to the bottom of the vent tower, the heavy dirty oil 6 at the bottom of the vent tower is pumped out by a vent tower bottom pump G and is sent to a vent tower bottom cooler F for cooling, one part of the heavy dirty oil returns to the tower to be cooled and absorbed by oil under the control of a heavy dirty oil reflux control valve J3, and the other part of the heavy dirty oil is sent out of the device under the control of a liquid level control valve J4 at the bottom of the vent tower. And (3) discharging vent tower top gas 7 consisting of steam and oil gas from the vent tower top, cooling to about 60 ℃ in a vent tower top cooler E, and then feeding into a vent tower top liquid separation tank D to separate out sewage 8, light sump oil 9 and non-condensable gas 10. The non-condensable gas 10 enters a torch discharge system, the sewage 8 is sent to an acidic water stripping device through a sewage pump H, and the light dirty oil 9 is sent out of the device through a dirty oil pump I.
At present, the problem of heavy oil carrying of an emptying tower commonly exists in a delayed coking device at home and abroad, and the heavy oil carrying of the emptying tower means that heavy oil at the bottom of the emptying tower is carried to the top of the emptying tower by gas when the heavy oil is cooled to the top of the emptying tower to be in contact with high-temperature oil gas for heat exchange and heavy oil absorption. The main hazards carried by heavy oil are: (1) heavy oil enters the overhead air cooler or the water cooler from the top of the emptying tower, and the heavy oil is unevenly solidified on the inner wall of the tube bundle, so that the heat transfer coefficient is reduced, even the tube bundle is blocked, the air cooler is caused to deflect, the pressure drop is increased, the temperature of the cooled gas is high, and the like. (2) The cooling temperature of oil gas is higher, and high-temperature oil gas containing a large amount of steam enters a torch system to influence the normal operation of the torch system. (3) The density of the heavy oil fraction is close to that of water, the heavy oil fraction contained in the top gas of the emptying tower can cause serious oil-water emulsification in a liquid separating tank at the top of the emptying tower, sewage and dirty oil can not be effectively separated, the oil content of the sewage is high, and the requirement of an externally-sent acid water stripping device can not be met; high water content of dirty oil, difficult recycling and the like. (4) Heavy oil at the bottom of the emptying tower is carried to the top of the tower, so that the cooling oil amount flowing back downwards in the tower is reduced, the contact cooling effect in the emptying tower is reduced, the liquid level at the bottom of the emptying tower is reduced, and the bottom pump is easy to evacuate. In conclusion, the problem of heavy oil carryover in the vent tower can seriously affect the safe, smooth and long-term operation of the vent system and even the coking unit.
Disclosure of Invention
The invention provides a method for reducing heavy oil carrying of an emptying tower of a delayed coking device, which can effectively reduce heavy oil carrying in the emptying tower, improve the operation of a steam blowing emptying and coke cooling system of the delayed coking device, prolong the operation period of the device and improve the operation safety of the device.
The invention provides a method for reducing heavy oil carrying of an emptying tower of a delayed coking device, which is realized by the following technical scheme:
(1) the method comprises the following steps that a water injection atomizer is arranged on an emptying gas pipeline at the outlet of a coke tower, when the coke tower is in a stage of atmospheric steam blowing and water supply coke cooling, atomized water is injected into the emptying gas pipeline through the water injection atomizer, high-temperature emptying gas in a pipeline is cooled by utilizing gasification heat of water, the temperature of the emptying gas and condensation of heavy dirty oil are realized, and the temperature of oil gas entering the emptying tower is reduced by adjusting the injection amount of water so as to reduce the air speed of the emptying tower in the emptying tower; arranging an emptying tower bottom oil heater, returning heavy sump oil at the bottom of a stock tower at the outlet of an emptying tower bottom pump to the emptying tower bottom oil heater for heating, and maintaining the temperature of a liquid phase entering the emptying tower so as to avoid sudden boiling of the tower bottom caused by water in the liquid phase; a pressure control valve is arranged on a non-condensable gas pipeline at the outlet of the liquid separating tank at the top of the emptying tower, so that the pressure at the top of the emptying tower is improved when the coke tower blows steam and is emptied, and the gas velocity of an empty tower in the emptying tower is reduced; and a washing baffle is arranged in the tower, and the heavy oil in the oil gas is further washed by high-temperature heavy oil.
(2) When the coke tower is in the stages of large steam blowing and water supply and coke cooling, water is injected into the emptying gas pipeline through the water injection atomizer, and the water is atomized by the water injection atomizer and then injected into the emptying gas.
(3) The temperature of oil gas entering the emptying tower is controlled to be 150-250 ℃ through the water injection amount in the emptying gas pipeline.
(4) And the pressure at the top of the emptying tower is increased to 0.15-0.20 MPag by adjusting a pressure control valve on a non-condensable gas pipeline at the outlet of a liquid separating tank at the top of the emptying tower.
(5) The liquid phase temperature of the material flow entering the emptying tower is controlled to be 150-250 ℃ by adjusting the flow of the heating medium.
(6) The washing heavy dirty oil in the emptying tower is heavy oil at 150-250 ℃ at the bottom of the emptying tower without being cooled, so that the absorption of water in the washing process is reduced, and the sudden boiling caused by the water entering the bottom of the emptying tower is avoided.
(7) And a pressure control valve is arranged on a noncondensable gas pipeline of the gas-liquid separation tank at the top of the emptying tower, and the pressure of the gas-liquid separation tank at the top of the emptying tower is adjusted to be stable.
(8) In order to avoid water carried by the emptying tower bottom oil from causing water bumping towards the tower or evacuation of a tower bottom pump, an emptying tower bottom oil circulating heater is arranged, and the emptying tower bottom oil is pumped out by a pump, is heated by a heating medium under the control of a flow regulating valve, returns to an inlet pipeline of the emptying tower and automatically flows to the emptying tower. And a liquid-phase thermocouple is arranged at the lower part of the inlet pipeline of the emptying tower and is used for measuring the temperature of the liquid phase of the material flow entering the emptying tower and controlling the flow of the heating medium through the temperature of the liquid phase.
The invention relates to a method for reducing heavy oil carrying of an emptying tower of a delayed coking device, which comprises the following steps:
when the coke tower of the delayed coking device is used for blowing and emptying, a large amount of high-temperature (250-420 ℃) emptying gas consisting of oil gas and steam is generated by large steam blowing and coke cooling of the coke tower and flows out from the top of the coke tower. Sewage in the top tank of the emptying tower is pumped out by a sewage pump, and is sent to the water injection atomizer arranged on the emptying gas pipeline after being pressurized, the sewage is atomized in the emptying gas pipeline and fully exchanges heat with the emptying gas, and the emptying gas is cooled. The temperature of the gas entering the emptying tower is controlled to be 150-250 ℃ by automatically adjusting the flow of the sewage so as to reduce the empty tower gas velocity of the emptying tower.
Pumping out heavy dirty oil at the bottom of the emptying tower by a bottom pump of the emptying tower, and returning a part of the heavy dirty oil to the tower as absorption washing oil under the control of a heavy dirty oil reflux control valve; heating a part of oil heater at the bottom of the emptying tower by a heating medium, returning the heated oil heater to an inlet pipeline of the emptying tower, automatically flowing the heated oil heater to the emptying tower, controlling the liquid phase temperature of material flow at the inlet of the emptying tower to be 150-; and the other part is cooled by a cooler at the bottom of the emptying tower and then is sent out of the device under the cascade control of the liquid level at the bottom of the emptying tower and the flow of the heavy dirty oil.
The uncooled heavy dirty oil serving as absorption washing oil is distributed through a heavy dirty oil distributor and is then redistributed, contacted and absorbed and washed through a heat exchange plate in the tower, and the heavy oil content of the gas phase at the top of the emptying tower is reduced.
The pressure control on the noncondensable gas pipeline of the gas-liquid separation tank at the top of the emptying tower is adjusted according to different stages of the atmospheric blowing of the coke tower and the water supply coke cooling so as to stabilize the operating pressure of the emptying tower between 0.15 and 0.2 MPag.
The method for reducing heavy oil carrying of the emptying tower of the delayed coking device has the advantages that high-temperature emptying gas from a coke tower and atomized sewage fully exchange heat, the temperature of the emptying gas entering the emptying tower is reduced, firstly, gas-phase heavy oil fractions in the emptying gas are condensed into liquid phases due to the reduction of the temperature, the gas-liquid phases are primarily separated through an emptying gas pipeline, liquid-phase heavy oil fractions in material flows entering the emptying tower directly fall to the bottom of the tower, and heavy oil fractions in the gas phases of the material flows entering the emptying tower are greatly reduced; and secondly, due to the reduction of the temperature, the gas density is increased under the same pressure, the volume flow is reduced, the gas velocity of an empty tower is reduced, and the heavy oil carrying is reduced.
A heavy dirty oil distributor is arranged in the emptying tower, so that the heavy dirty oil is distributed more uniformly in the range of the cross section of the tower; the gas and liquid phases in the emptying tower are redistributed and contacted for multiple times to absorb by matching with the heat exchange plate, so that the washing effect of heavy dirty oil on the gas phase in the tower is enhanced, and the heavy oil carrying is reduced.
In the process of blowing steam and emptying of the existing delayed coking device, non-condensable gas in a liquid separation tank at the top of an emptying tower is directly discharged to a torch system without pressure control, and the pressure of the liquid separation tank at the top of the emptying tower is about 0.05 MPag. According to the invention, when the flow rates of the large steam blowing water and the cold coke water feeding are larger and the temperature of the gas outlet at the top of the coke tower is higher, the pressure of the liquid separation tank at the top of the emptying tower is maintained to be 0.15-0.2MPag, so that the pressure of the emptying tower is increased, the gas phase density in the emptying tower is increased, the gas velocity of the emptying tower is reduced by about 50%, the heavy oil sedimentation and washing absorption are facilitated, and the heavy oil carrying of oil gas is also facilitated to be reduced.
The emptying tower bottom oil is heated by the emptying tower bottom heater to maintain the temperature of the emptying tower bottom oil, so that the phenomenon that steam is partially supercooled into water drops and falls into the tower bottom because the cold emptying tower bottom oil is used as washing oil is avoided, and when the tower bottom oil is rapidly heated, water bumping is caused, so that heavy oil fractions are carried to an emptying tower top system in a large quantity, the tower top system is blocked, a tower bottom pump is pumped out, and the normal operation of the device is influenced.
The method achieves the purpose of reducing the heavy oil carrying of the emptying tower by the comprehensive means.
Drawings
FIG. 1: schematic process flow diagram of steam blowing and emptying stage of existing delayed coking device
FIG. 2 is a drawing: the invention discloses a process schematic diagram of a method for reducing carrying of empty tower heavy oil in a delayed coking device
Description of reference numerals:
equipment: A. a green coke tower B, a decoking coke tower C, an emptying tower D and an emptying tower top liquid separating tank
E. An emptying tower top cooler F, an emptying tower bottom cooler G, an emptying tower bottom pump H and a sewage pump
I. Sump oil pump J1, gas phase thermocouple J2, emptying tower inlet gas phase temperature-sewage flow control valve J3, heavy sump oil reflux amount control valve J4, emptying tower bottom liquid level-heavy sump oil outlet device amount flow control valve J5, steam supply flow control valve J6, water supply flow control valve J7, emptying tower top tank pressure control valve J8, liquid phase thermocouple J9, liquid phase temperature-heating medium control valve J10, circulating oil flow control valve K, four-way valve L1, coke tower A side feed block valve L2, coke tower B side feed block valve M1, coke tower A side oil throwing main valve M2, coke tower B side oil throwing main valve N1, coke tower A side bottom steam blowing valve N2, coke tower B side bottom steam blowing valve O1, coke tower A side bottom valve O2, coke tower B side bottom water supply valve P1, coke tower A side large oil gas block valve P2, A big oil-gas isolating valve R1 at the side of the coke tower B, a side-blown steam-emptying isolating valve R2 of the coke tower A, a side-blown steam-emptying isolating valve S of the coke tower B, a water injection atomizer T and an emptying tower bottom heater
Logistics: 1. coking oil 2, coking oil gas 3, vent gas 4, steam 5, cold coke water 6, heavy dirty oil 7, vent tower top gas 8, sewage 9, light dirty oil 10, non-condensable gas 11 and heating medium
Detailed Description
The method for reducing the carry-over of empty tower heavy oil in a delayed coking unit according to the present invention is described in further detail with reference to the accompanying FIG. 2:
as shown in fig. 2: set up water injection atomizer S on the blow-down gas pipeline of coke drum export, when the coke drum was in big blow steam and the cold burnt stage of feedwater, injected atomized water 8 into 3 pipelines of blow-down gas through water injection atomizer S, utilized the high temperature oil vapour in the gasification heat cooling pipeline of water, realized gaseous cooling and the condensation of heavy dirty oil.
The water injection atomizer S is composed of an atomizing nozzle, a connecting pipe, a flange and a supporting frame, the installation position of the atomizer S is located on a coke tower top to a vent gas 3 header pipe of a vent tower C, the installation position is far away from the inlet position of the vent tower C as far as possible, the nozzle of the atomizer S is located at the axis position of a vent gas pipeline, and the injection direction is consistent with the flow direction of vent gas.
A thermocouple J1 for measuring temperature is arranged on the upper part of the vent gas 3 pipeline at the downstream of the atomizer S in the flow direction of the vent gas 3, and a thermocouple J1 is arranged at the position which is at least 10 times of the diameter of the vent gas pipeline at the downstream of the position where the water injection atomizer S is arranged. Temperature thermocouple J1 measures the gas phase temperature in the line of vent gas 3. And a water injection flow control valve J2 is arranged, and the gas phase temperature in the air emptying gas pipeline is controlled to be 200 ℃ through water injection flow. The water injection is firstly selected from sewage separated by a liquid separating tank at the top of the emptying tower, and other sewage or clean water which can be provided in an oil refinery can also be adopted.
The inside heavy dirty oil distributor and the umbrella type + slope ring type combination heat transfer board that set up of evacuation tower C, heavy dirty oil sprays downwards through heavy dirty oil distributor, cools off and washes the absorption through combination heat transfer board to the gas that empties. The umbrella-shaped and inclined circular ring-shaped combined heat exchange plate has enough strength and heat exchange effect.
A pressure control valve J7 is arranged on a noncondensable gas pipeline of the gas-liquid separation tank D at the top of the emptying tower, the pressure of the gas-liquid separation tank D at the top of the emptying tower is adjusted according to the large steam blowing and cold coke water supply amount in the large steam blowing and water supply and cold coke cooling stages of the coke tower, and the higher pressure is controlled to be 0.15-0.2MPag when the large steam blowing and cold coke water supply flow is larger and the outlet temperature of the gas at the top of the coke tower is higher; on the contrary, when the flow rates of the large steam blowing water and the cold coke water feeding are small and the temperature of the gas outlet at the top of the coke tower is low, the lower pressure is controlled to be 0.05-0.15 MPag.
In order to avoid water carried by the emptying tower bottom oil 7 from causing water to suddenly boil and flush the tower or the emptying of the tower bottom pump G, an emptying tower bottom oil circulating heater T is arranged, and the emptying tower bottom oil 7 is pumped out by a pump, is heated by a heating medium 11 under the control of a flow regulating valve J10, returns to an emptying tower inlet pipeline and automatically flows to the emptying tower. And a liquid-phase thermocouple J8 is arranged at the lower part of the inlet pipeline of the vent tower and is used for measuring the temperature of the liquid phase of the material flow entering the vent tower and controlling the flow of the heating medium through the temperature of the liquid phase.
The green coke tower A is in a green coke stage, the four-way valve K points to the green coke tower A, and the feeding isolating valve L1 on the side of the coke tower A is opened; closing an oil throwing main valve M1 at the side A of the coke tower; closing a bottom steam blowing valve N1 on the side of the coke tower A; coke drum a side bottom feed valve O1 is closed; opening a large oil-gas isolating valve P1 on the side of the coke tower A; coke drum a side blow blowdown block valve R1 is closed. The coking oil 1 from the coking heating furnace enters a raw coke tower A through a four-way valve K, a series of cracking and condensation reactions occur in the coke tower, the coke generated by the reactions is left in the coke tower, the coking oil gas 2 produced by the reactions flows out from the top of the coke tower, and is quenched by quenching oil and then enters a fractionation system to separate different fractions.
When the green coke of the decoking coke tower B is in a steam blowing and emptying stage, a side feeding isolating valve L2 of the coke tower B is closed; opening an oil throwing main valve M2 at the side B of the coke tower; closing a large oil-gas isolating valve P2 at the side B of the coke tower; coke drum B side blow and vent block valve R2 is opened. When decoking coke drum B is undergoing a large blow operation: the bottom steam blowing valve N2 on the side of the coke tower B is opened; coke drum a side bottom feed valve O2 is closed; when decoking coke drum B is undergoing feedwater cooling operations: coke drum B side bottom blow valve N2 was closed; coke drum B side bottom feed valve O2 is opened.
And a large amount of high-temperature (250-420 ℃) vent gas 3 generated by the large steam blowing and the cold coke of the decoking coke tower B flows out from the top of the coke tower. The sewage 8 is injected into the vent gas 3 through the water injection atomizer S, and the vent gas 3 is cooled. The flow of the sewage 8 is adjusted by a gas phase temperature-sewage flow control valve J2 at the inlet of the emptying tower, and the temperature of the oil gas entering the emptying tower is controlled to be 200 ℃. Cooling the gas phase heavy oil fraction in the vent gas 3 into a liquid phase, separating the gas phase and the liquid phase through an inlet pipeline of a vent tower C, and directly dropping the liquid phase heavy oil fraction into the bottom of the tower after entering the vent tower 3, so that the heavy oil fraction in the gas phase in the vent tower is greatly reduced; the gas phase in the emptying column C is further washed with heavy oil fraction via heavy dirty oil 6.
The heavy dirty oil 6 at the bottom of the emptying tower is pumped out by a pump G at the bottom of the emptying tower, and part of the heavy dirty oil is used as washing oil to return to the tower under the control of a heavy dirty oil return flow control valve J3; heating a part of bottom oil heater T to the emptying tower by a heating medium 11, returning to an inlet pipeline of the emptying tower, automatically flowing to the emptying tower C, and controlling the heavy sump oil to be heated to 200 ℃ by a liquid phase temperature-heating medium control valve; and the other part is cooled by a vent tower bottom cooler F and discharged out of the device under the control of a vent tower bottom liquid level-heavy dirty oil discharging device flow control valve J4.
And (3) discharging vent tower top gas 7 consisting of steam and oil gas from the vent tower top, cooling to about 60 ℃ in a vent tower top cooler E, and then entering a vent tower top liquid separation tank D to separate out sewage 8, light sump oil 9 and non-condensable gas 10. The pressure of the emptying tower top tank is controlled to be 0.18MPag by the pressure control valve J7 of the emptying tower top tank, and the non-condensable gas 10 is discharged to a torch discharge system after being subjected to pressure control. The light dirty oil 9 is sent out of the device through a dirty oil pump I. And one part of the sewage 8 is sent to a cold coke pool or an acidic water stripping device by a sewage pump H, and the other part of the sewage is sent to a water injection atomizer S on an emptying gas line, so that the gas phase temperature of the material flow at the inlet of the emptying tower is controlled.
Examples
The 100-million-ton/year delayed coking device emptying tower of a certain domestic refinery has serious heavy oil carrying problems, so that air cooling and wax precipitation at the top of the emptying tower are caused, the cooling capacity at the top of the emptying tower is insufficient, non-condensable gas at the top of a liquid separation tank at the top of the emptying tower cannot be discharged to a torch, the normal production of the delayed coking device is seriously influenced, and the device is forced to be stopped once every half year to coke the air cooler. After the refinery is transformed by the method for reducing the carrying of the empty tower heavy oil by the delayed coking device, the problem of the carrying of the heavy oil by the empty tower is effectively solved, the coke cleaning frequency of an air cooler at the top of the emptying tower is reduced to three years/time per operation cycle from half a year/time, the cooling capacity at the top of the emptying tower can be effectively exerted, the oil-water emulsification phenomenon of a liquid separating tank at the top of the emptying tower is effectively relieved, and the long-period safe and stable operation of the device is ensured.
Claims (6)
1. A method for reducing heavy oil carrying of an emptying tower of a delayed coking device is characterized by comprising the following steps: when the coke tower is in a stage of large steam blowing and water supply and coke cooling, water is injected into the emptying gas pipeline, high-temperature oil steam in the pipeline is cooled by utilizing gasification heat of water, the temperature of gas is reduced, heavy dirty oil is condensed, and the temperature of oil gas entering the emptying tower is controlled by adjusting the injection amount of water; arranging an emptying tower bottom oil heater, heating one strand of tower bottom heavy dirty oil at the outlet of an emptying tower bottom pump to the emptying tower bottom oil heater, and returning to an inlet pipeline of the emptying tower; a pressure control valve is arranged on a noncondensable gas pipeline at the outlet of the liquid separating tank at the top of the emptying tower, and the pressure at the top of the emptying tower is adjusted when the coke tower blows steam and is emptied; when the flow rates of the large steam blowing water and the cold coke water feeding are high and the temperature of the gas outlet at the top of the coke tower is high, controlling the pressure to be 0.15-0.2 MPag; when the flow rates of the large steam blowing and the cold coke water feeding are small and the temperature of the gas outlet at the top of the coke tower is low, the pressure is controlled to be 0.05-0.15 MPag;
a heavy dirty oil distributor is arranged in the emptying tower, and the heavy dirty oil is sprayed downwards through the heavy dirty oil distributor; and a heat exchange plate is arranged in the emptying tower, and the heat exchange plate adopts an umbrella-shaped and inclined annular combined heat exchange plate.
2. The method for reducing carry over of heavy oil in an emptying tower of a delayed coking device according to claim 1, wherein the method comprises the following steps: when the coke tower is in the stages of large steam blowing and water supply and coke cooling, water is injected into the emptying gas pipeline through the water injection atomizer, and water is atomized by the atomizer and then injected into the emptying gas.
3. The method for reducing carry over of heavy oil in an emptying tower of a delayed coking device according to claim 1, wherein the method comprises the following steps: the temperature of the oil gas entering the emptying tower is controlled to be 150-250 ℃.
4. The method for reducing carry over of heavy oil in an emptying tower of a delayed coking device according to claim 1, wherein the method comprises the following steps: the liquid phase temperature of the material flow entering the emptying tower is controlled to be 150-250 ℃ by adjusting the flow of the heating medium.
5. The method for reducing carry over of heavy oil in an emptying tower of a delayed coking device according to claim 1, wherein the method comprises the following steps: the inside heavy dirty oil distributor that sets up of blow-down tower, heavy dirty oil washing blow-down gas.
6. The method for reducing carry over of heavy oil in an emptying tower of a delayed coking device according to claim 1, wherein the method comprises the following steps: the water injection adopts desalted water, deoxygenated water, fresh water, sulfur-containing sewage, oil-containing sewage and water-containing dirty oil.
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