CN113462423A - Method for treating gas phase entrainment and flare system - Google Patents
Method for treating gas phase entrainment and flare system Download PDFInfo
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- CN113462423A CN113462423A CN202010247032.7A CN202010247032A CN113462423A CN 113462423 A CN113462423 A CN 113462423A CN 202010247032 A CN202010247032 A CN 202010247032A CN 113462423 A CN113462423 A CN 113462423A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/002—Cooling of cracked gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The application discloses a method for treating gas phase entrainment and a venting system, and belongs to the technical field of petroleum refining. According to the emptying system provided by the embodiment of the application, a part of oil phase from the circulating system is atomized into first oil phase liquid drops through the Venturi atomization scrubber, heavy fraction oil in steam is condensed into second oil phase liquid drops through the first oil phase liquid drops, coke powder in the steam is trapped through the first oil phase liquid drops and the second oil phase liquid drops, and the first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder are separated from a gas phase in the steam through the distributor. The device can separate heavy fraction and fine coke in the steam from the gas phase through the venturi atomization scrubber and the distributor, so that the heavy fraction and the fine coke are not carried in the gas phase output from the top of the emptying tower, the separation effect is improved, and the problems of safety and environmental protection, such as blockage of a cooling system, standard exceeding of temperature, poor oil-water separation effect and the like caused by gas phase entrainment in the emptying system are solved.
Description
Technical Field
The application relates to the technical field of petroleum refining. In particular to a method for processing gas phase entrainment and a venting system.
Background
In the technical field of petroleum refining, a venting system of a delayed coking device is generally adopted to process a large amount of steam from a coke tower, heavy distillate oil and coke powder in the steam are separated from gas through the venting system and then are respectively recovered, the steam contains gas phase, the heavy distillate oil and the coke powder, and the gas phase comprises non-condensable gas, water vapor and other oil gases.
The emptying system in the related technology mainly comprises an emptying tower, a three-phase separator, a cooling system and a circulating system, wherein the top of the emptying tower is connected with the cooling system, the cooling system is connected with the three-phase separator, and the bottom of the emptying tower is connected with the circulating system. Steam from the coke tower enters an emptying tower, heavy distillate oil and coke powder are separated from the bottom of the tower after being separated by a baffle in the emptying tower, and flow back to the top of the tower through a circulating system; the gas phase is output from the top of the tower, cooled by a cooling system and then separated by a three-phase separator.
However, the tower plates in the emptying tower are easy to fall off in the application process, so that incomplete separation is caused, a large amount of heavy distillate oil and coke powder are carried in the gas phase output from the top of the tower, and the separation effect is poor.
Disclosure of Invention
The embodiment of the application provides a method for processing gas phase entrainment and an emptying system, so that heavy fractions and coke powder are not carried in a gas phase output from the top of an emptying tower, and the separation effect is improved. The specific technical scheme is as follows:
in one aspect, an embodiment of the present application provides a venting system, where the venting system includes: the device comprises an emptying tower, a cooling system, a circulating system, a three-phase separator, a Venturi atomization scrubber and a distributor;
one end of the Venturi atomization scrubber is connected with the distributor, and the distributor is positioned in the emptying tower;
the bottom of the emptying tower is connected with one end of the circulating system, and the other end of the circulating system is connected with the other end of the Venturi atomization scrubber;
the top of the emptying tower is connected with one end of the cooling system, and the other end of the cooling system is connected with the first end of the three-phase separator;
the circulating system is used for refluxing a part of oil phase output from the tower bottom of the emptying tower to the Venturi atomization scrubber, and the oil phase comprises first oil phase liquid drops and second oil phase liquid drops, wherein coke powder is trapped in the first oil phase liquid drops and the second oil phase liquid drops;
the venturi atomization scrubber is used for atomizing a part of oil phase from the circulating system into first oil phase liquid drops, condensing heavy fraction oil in steam from a coke tower into second oil phase liquid drops through the first oil phase liquid drops, and trapping coke powder in the steam through the first oil phase liquid drops and the second oil phase liquid drops, wherein the steam comprises noncondensable gas, water vapor and other oil gases besides the heavy fraction oil and the coke powder;
the distributor is used for separating the first oil phase liquid drops and the second oil phase liquid drops which are trapped with coke breeze from the gas phase in the steam, wherein the gas phase comprises the non-condensable gas, the water vapor and the other oil gas;
the cooling system is used for cooling the gas phase output from the top of the emptying tower;
the three-phase separator is used for separating non-condensable gas, water vapor and other oil gas in the gas phase.
In one possible implementation, the emptying system further includes: a cyclone separator;
the cyclone separator is positioned in the emptying tower and above the distributor;
the cyclone separator is used for further separating heavy distillate oil and coke powder carried in the gas phase.
The cooling system includes: an air cooler and an aftercooler;
one end of the air cooler is connected with the top of the emptying tower, and the other end of the air cooler is connected with one end of the after-cooler;
the other end of the after-cooler is connected with the first end of the three-phase separator.
In another possible implementation, the circulation system includes: a circulating oil pump and a cooling water tank;
one end of the circulating oil pump is connected with the bottom of the emptying tower, and the other end of the circulating oil pump is connected with the first end of the cooling water tank;
the second end of the cooling water tank is connected with the other end of the Venturi atomization scrubber, and the third end of the cooling water tank is connected with a first conveying pipeline;
the circulating oil pump is used for conveying an oil phase output from the bottom of the emptying tower to the cooling water tank;
the first transfer line is for outputting another portion of the oil phase.
In another possible implementation manner, the emptying system further includes: a sump oil pump, a sump pump and a second transfer line;
the second end of the three-phase separator is connected with the sewage pump, the third end of the three-phase separator is connected with the sewage pump, and the fourth end of the three-phase separator is connected with the second conveying pipeline;
the dirty oil pump is used for conveying dirty oil separated by the three-phase separator, and the dirty oil comprises other oil gas;
the sewage pump is used for conveying the sewage separated by the three-phase separator, and the sewage comprises the water vapor;
the second conveying pipeline is used for conveying the non-condensable gas separated by the three-phase separator.
In another possible implementation manner, the emptying system further includes: flow meters and thermometers;
the circulating system is connected with the Venturi atomization scrubber through a third conveying pipeline, and the flow meter is positioned on the third conveying pipeline;
one end of the thermometer is connected with the flowmeter, and the other end of the thermometer is connected with the emptying tower;
the flow meter is used for monitoring the flow of the oil phase input into the Venturi atomization scrubber from the circulating system;
the thermometer is used for monitoring the temperature of the emptying tower.
In another aspect, embodiments of the present application provide a method for treating gas phase entrainment, the method including:
atomizing a portion of an oil phase from a circulation system into first oil phase droplets by a venturi atomization scrubber, mixing the first oil phase droplets with steam from a coke drum in the venturi atomization scrubber, condensing heavy fraction oil in the steam into second oil phase droplets by the first oil phase droplets, the oil phase comprising first oil phase droplets and second oil phase droplets with trapped coke fines;
capturing the coke fines in the steam by the first oil phase droplets and the second oil phase droplets;
separating the first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder from the gas phase in the steam through a distributor in the emptying tower;
and outputting the separated gas phase from the top of the emptying tower, and outputting the separated first oil phase liquid drop and the second oil phase liquid drop which are collected with the coke powder as oil phases from the bottom of the emptying tower, wherein the gas phase comprises non-condensable gas, water vapor and other oil gases.
In one possible implementation, before the outputting the separated gas phase from the top of the emptying column, the method further includes:
and further separating heavy fraction oil and coke powder carried in the gas phase by a cyclone separator in the emptying tower.
In another possible implementation manner, the method further includes:
monitoring the flow rate of the oil phase refluxed into the venturi atomization scrubber by a flow meter;
monitoring the temperature of the evacuation tower by a thermometer;
the temperature of the vent tower is adjusted by varying the flow of oil phase back into the venturi atomization scrubber.
In another possible implementation manner, the method further includes:
cooling a gas phase output from the top of the evacuation column by a cooling system;
and refluxing one part of the oil phase output from the bottom of the emptying tower to the Venturi atomization scrubber through the circulating system, and outputting the other part of the oil phase through a first conveying pipeline.
In another possible implementation manner, the method further includes:
conveying the gas phase cooled by the cooling system to a three-phase separator;
separating non-condensable gases, water vapor and other oil and gas in the gas phase by the three-phase separator;
the noncondensable gas of separation is carried through the second pipeline, carries the sump oil of separation through the sump oil pump to and carry the sewage of separation through the sump oil pump, include in the sump oil other oil gas, include in the sewage vapor.
The technical scheme provided by the embodiment of the application has the following beneficial effects:
the emptying system that this application embodiment provided, including the emptying tower, cooling system, the circulation system, the three-phase separator, venturi atomization scrubber and distributor, will come from a part oil phase of circulation system to atomize into first oil phase liquid drop through venturi atomization scrubber, will come from the heavy-duty oil condensation in the steam of coke drum into second oil phase liquid drop through first oil phase liquid drop, catch the coke breeze in the steam through first oil phase liquid drop and second oil phase liquid drop, will catch the first oil phase liquid drop and the second oil phase liquid drop that have the coke breeze and leave with the gaseous phase in the steam through the distributor, and then through cooling system cooling gaseous phase, through the noncondensable gas, vapor and other oil gas in the three-phase separator separation gaseous phase. The device can separate heavy fraction and fine coke in the steam from the gas phase through the venturi atomization scrubber and the distributor, so that the heavy fraction and the fine coke are not carried in the gas phase output from the top of the emptying tower, the separation effect is improved, and the problems of safety and environmental protection, such as blockage of a cooling system, standard exceeding of temperature, poor oil-water separation effect and the like caused by gas phase entrainment in the emptying system are solved.
Drawings
FIG. 1 is a schematic diagram of an evacuation system provided by an embodiment of the present application;
FIG. 2 is a schematic view of another flare system provided by an embodiment of the present application;
FIG. 3 is a flow chart of a method for handling gas phase entrainment according to an embodiment of the present disclosure.
The reference numerals denote:
1-an emptying tower, 2-a cooling system, 3-a circulating system, 4-a three-phase separator, 5-a Venturi atomization scrubber,
6-distributor, 7-cyclone separator, 8-sump oil pump, 9-sump oil pump, 10-second conveying pipeline, 11-flowmeter,
12-thermometer, 13-pressure control valve, 21-air cooler, 22-aftercooler, 31-circulating oil pump,
32-cooling water tank, 33-first transfer line.
Detailed Description
In order to make the technical solutions and advantages of the present application more clear, the following describes the embodiments of the present application in further detail.
An embodiment of the present application provides a venting system, see fig. 1, including: the device comprises a vent tower 1, a cooling system 2, a circulating system 3, a three-phase separator 4, a Venturi atomization scrubber 5 and a distributor 6;
one end of the Venturi atomization scrubber 5 is connected with a distributor 6, and the distributor 6 is positioned in the emptying tower 1;
the bottom of the emptying tower 1 is connected with one end of a circulating system 3, and the other end of the circulating system 3 is connected with the other end of a Venturi atomization scrubber 5;
the top of the emptying tower 1 is connected with one end of a cooling system 2, and the other end of the cooling system 2 is connected with the first end of a three-phase separator 4;
the circulating system 3 is used for refluxing a part of oil phase output from the tower bottom of the emptying tower 1 to the Venturi atomizing scrubber 5, and the oil phase comprises first oil phase liquid drops and second oil phase liquid drops which are used for trapping coke powder;
the Venturi atomization scrubber 5 is used for atomizing a part of oil phase from the circulating system 3 into first oil phase liquid drops, condensing heavy fraction oil in steam from a coke tower into second oil phase liquid drops through the first oil phase liquid drops, and trapping coke powder in the steam through the first oil phase liquid drops and the second oil phase liquid drops, wherein the steam comprises noncondensable gas, water vapor and other oil gases besides the heavy fraction oil and the coke powder;
the distributor 6 is used for separating the first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder from non-condensable gas, water vapor and other oil gas in the steam;
the cooling system 2 is used for cooling noncondensable gas, steam and other oil gas output from the top of the emptying tower 1;
the three-phase separator 4 is used for separating non-condensable gas, water vapor and other oil gas.
In the related technology, a plurality of layers of herringbone or duckbill baffles are arranged in the emptying tower 1, and a heat exchange space is provided through the baffles, so that heavy fraction oil and coke powder in steam are condensed. However, in actual production, the baffle falls off seriously, which causes the reduction of the separation efficiency of the emptying tower 1 and the reduction of the washing effect of coke powder, leads a large amount of heavy distillate oil and coke powder to enter the top of the emptying tower 1, and the heavy distillate oil and the coke powder become liquid phase with high specific gravity and high viscosity when passing through the cooling system 2, and are easy to adhere to the pipe wall, namely, paraffin is formed in the production, and then the shutdown and maintenance are frequent due to the influence on the heat exchange effect. Because the baffle drops and leads to the heat transfer effect unable assurance, the temperature of the gaseous phase that gets into in three phase separator 4 can not reach the requirement, can carry more vapor in the noncondensable gas, leads to the torch of unloading to extinguish the accident. More seriously, the oil-water emulsification is serious, the density difference is very small, and the three-phase separator 4 loses the oil-water separation function, so that the oil and the water are mixed. In the related art, the sewage separated by the three-phase separator 4 is generally conveyed to the acid water stripping device, and the dirty oil is conveyed to the dirty oil tank, and when the above occurs, the separation effect of the three-phase separator 4 is poor, and the pollution is diffused to the tank area and the acid water stripping device. In addition, in the related technology, sewage is sometimes conveyed to a coke cooling water system for recycling, but due to poor separation effect and excessive sewage, the sewage can be recycled in the coke cooling water system for a long time, so that hydrogen sulfide is accumulated, peculiar smell is serious, and serious environmental protection problems are caused.
In the embodiment of the application, the oil phase is atomized into the first oil phase liquid drops by adopting a quenching technology in the venturi atomization scrubber 5, the oil phase is mainly heavy distillate oil, the first oil phase liquid drops have a large specific surface area and a low temperature, the first oil phase liquid drops and steam from a coke tower are fully mixed, cooled and absorbed, the temperature of the heavy distillate oil in the steam is reduced to a condensation temperature to form the second oil phase liquid drops, and the gradually increased first oil phase liquid drops and the second oil phase liquid drops are fully used for capturing coke powder in the steam in the venturi atomization scrubber 5 through a dust washing technology of a venturi reducing section and a diffusion section. And then the first oil phase liquid drop and the second oil phase liquid drop which are trapped with the coke powder are separated from the gas phase in the steam by the distributor 6 in the emptying tower 1, wherein the gas phase comprises non-condensable gas, water vapor and other oil gas, so that the heavy fraction and the coke powder are not carried in the gas phase output from the top of the emptying tower 1, the separation effect is improved, and the problems of safety and environmental protection, such as blockage of a cooling system 2, standard exceeding of temperature, poor oil-water separation effect and the like caused by gas phase entrainment in an emptying system are solved.
It should be noted that the distributor 6 can further prevent the uneven impingement of the steam and reduce the damage to the internals. In addition, the emptying tower 1 provided by the embodiment of the application is not provided with a baffle.
Introduction of the cyclone 7: in one possible implementation, referring to fig. 2, the venting system further comprises: a cyclone separator 7;
the cyclone separator 7 is positioned in the emptying tower 1 and above the distributor 6;
the cyclone separator 7 is used for further separating heavy distillate oil and coke powder entrained in the gas phase.
In the embodiment of the application, the first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder enter the distributor 6 of the emptying tower 1 together with other components in the steam, in the distributor 6, the larger oil phase liquid drops directly fall to the bottom of the emptying tower 1, and the smaller oil phase liquid drops possibly ascend with the gas phase in the steam, so that heavy fraction oil and coke powder are still entrained in the gas phase. In the implementation mode, the cyclone 7 is additionally arranged in the emptying tower 1, and the small oil phase liquid drops are separated from the gas phase in the steam again through the cyclone 7, so that the gas phase output from the top of the tower is clean, heavy distillate oil and coke powder are not carried, and the problems of safety and environmental protection, such as blockage of a cooling system 2, standard exceeding of temperature, poor oil-water separation effect and the like caused by gas phase entrainment in an emptying system are solved.
The cyclone separator 7 provided by the embodiment of the application can realize the separation efficiency of more than 99%, and realize no entrainment of the gas phase at the top of the tower.
The distance between the cyclone 7 and the distributor 6 can be set and changed as required, and is not particularly limited in the embodiment of the present application.
Introduction of cooling system 2: in one possible implementation, the cooling system 2 comprises: an air cooler 21 and an aftercooler 22;
one end of the air cooler 21 is connected with the top of the emptying tower 1, and the other end of the air cooler 21 is connected with one end of the aftercooler 22;
the other end of the aftercooler 22 is connected to a first end of the three-phase separator 4.
In this implementation, the gas phase output from the top of the vent tower 1 is cooled by the air cooler 21, condensed and cooled by the aftercooler 22, and then the cooled gas phase is input to the three-phase separator 4 for further separation, wherein the gas phase includes non-condensable gas, water vapor and other oil and gas.
Air cooler 21 uses ambient air as coolant, in this implementation, carries out preliminary cooling, cooling to the gaseous phase through air cooler 21 earlier, and the gaseous phase is further cooled through aftercooler 22 to the rethread. The aftercooler 22 has a small volume, a small pitch, a very uniform temperature distribution and a good cooling effect.
Introduction of the circulation system 3: in one possible implementation, the circulation system 3 comprises: a circulation oil pump 31 and a cooling water tank 32;
one end of the circulating oil pump 31 is connected with the bottom of the emptying tower 1, and the other end of the circulating oil pump 31 is connected with the first end of the cooling water tank 32;
the second end of the cooling water tank 32 is connected with the other end of the Venturi atomization scrubber 5, and the third end of the cooling water tank 32 is connected with a first conveying pipeline 33;
the circulating oil pump 31 is used for conveying the oil phase output from the bottom of the emptying tower 1 to the cooling water tank 32;
the first transfer line 33 is used to output another part of the oil phase.
In this implementation, the oil phase output from the bottom of the evacuation tower 1 is output to the cooling water tank 32 through the circulating oil pump 31, the oil phase mainly includes heavy distillate oil, after the oil phase is cooled in the cooling water tank 32, a part of the oil phase is output to the venturi atomization scrubber 5, the part of the oil phase is atomized again into oil phase droplets through the venturi atomization scrubber 5, and the other part of the oil phase is output through the first delivery line 33.
In one possible implementation, the further portion of the oil phase may be transferred to the sump tank via a first transfer line 33; in another possible implementation, it may also be sent to the fractionation column for recycling through the first transfer line 33. In the embodiments of the present application, this is not particularly limited.
Wherein the water in the cooling water tank 32 may be circulating water from other devices.
In one possible implementation, the evacuation system further includes: a sump oil pump 8, a sump pump 9 and a second transfer line 10;
the second end of the three-phase separator 4 is connected with a sewage pump 8, the third end of the three-phase separator 4 is connected with a sewage pump 9, and the fourth end of the three-phase separator 4 is connected with a second conveying pipeline 10;
the dirty oil pump 8 is used for conveying dirty oil separated by the three-phase separator 4, and the dirty oil comprises other oil gas;
the sewage pump 9 is used for conveying the sewage separated by the three-phase separator 4, and the sewage comprises water vapor;
the second transfer line 10 is used for transferring the non-condensable gases separated by the three-phase separator 4.
The three-phase separator 4 is mainly used for separating oil, gas and water, and can accurately measure the yield of the oil, gas and water. The form of the three-phase separator 4 may be arranged and modified as needed, and in the embodiment of the present application, this is not particularly limited, for example, the three-phase separator 4 is a vertical separator, a horizontal separator, or a spherical separator.
The gas phase condensed and cooled by the air cooler 21 and the aftercooler 22 enters the three-phase separator 4 from the first end of the three-phase separator 4, is separated in the three-phase separator 4, and the separated sump oil is output from the second end of the three-phase separator 4 and is conveyed by the sump oil pump 8; the separated sewage is output from the third end of the three-phase separator 4 and is conveyed by a sewage pump 9; the separated non-condensable gases are transported via a second transport line 10.
In a possible implementation manner, the dirty oil delivered by the dirty oil pump 8 can be input into the dirty oil tank or the fractionating tower together with another part of the oil phase output from the cooling water tank 32, the sewage delivered by the dirty oil pump 9 can be input into the acidic water stripping device through the delivery pipeline for treatment, the non-condensable gas delivered by the second delivery pipeline 10 can be recovered, and the non-condensable gas can be discharged after being combusted by the emptying torch, so that the pollution to the environment is avoided.
It should be noted that the emptying system provided by the embodiment of the present application can fundamentally solve the problem of gas phase entrainment, heavy fraction oil and coke powder do not enter the tower top, and the operation of the cooling system 2 is ensured. The speed of the steam entering the emptying tower 1 is greatly reduced, the impact on the distributor 6 and the cyclone separator 7 in the tower is small, and the internal parts are stable and do not fall off. The separation effect of oil, gas and water in the three-phase separator 4 is good, and the sulfur-containing sewage can be directly conveyed to the acidic water stripping device without open discharge, thereby meeting the requirements of the current environmental protection policy and regulations. And the temperature of the three-phase separator 4 is low, the water content in the non-condensable gas is low, and the recovery or emptying torch is safer. And the requirement of long-period operation of the oil refining device can be met.
Introduction of flowmeter 11 and thermometer 12: in one possible implementation, the evacuation system further includes: a flow meter 11 and a thermometer 12;
the circulating system 3 is connected with the Venturi atomization scrubber 5 through a third conveying pipeline, and the flow meter 11 is positioned on the third conveying pipeline;
one end of a thermometer 12 is connected with the flowmeter 11, and the other end of the thermometer 12 is connected with the emptying tower 1;
the flow meter 11 is used for monitoring the flow of the oil phase from the circulating system 3 to the venturi atomization scrubber 5;
the thermometer 12 is used to monitor the temperature of the evacuation tower 1.
In this implementation, the flow rate of the oil phase input into the venturi atomization scrubber 5 is monitored by the flow meter 11, the temperature in the evacuation tower 1 is monitored by the thermometer 12, and the temperature in the evacuation tower 1 can be adjusted by adjusting the flow rate of the oil phase, so that the temperature is favorable for improving the separation effect of the distributor 6 and the cyclone 7. When the flow of the oil phase is larger, the temperature of the emptying tower 1 is lower; when the flow rate of the oil phase is small, the temperature of the evacuation tower 1 is high. When the temperature in the emptying tower 1 is low, the separation of heavy fraction, coke powder and gas phase is facilitated, the separation effect is improved, the temperature of the gas phase entering the three-phase separator 4 is reduced, and the separation effect of the three-phase separator 4 is improved.
In a possible embodiment, a thermometer 12 can also be provided on the line which leads off the gas phase from the top of the vent column 1, the temperature of the gas phase being monitored by means of the thermometer 12.
In another possible implementation, a liquid level meter and a regulating valve are arranged on a pipeline for conveying sewage through the sewage pump 9, the regulating valve is positioned on the pipeline for conveying sewage, one end of the liquid level meter is connected with the regulating valve, the other end of the liquid level meter is connected with the three-phase separator 4, the liquid level of sewage in the three-phase separator 4 is monitored through the liquid level meter, and the flow rate of conveying sewage is regulated through the regulating valve based on the liquid level of sewage in the three-phase separator 4. Also can be equipped with level gauge and governing valve on the pipeline of carrying the sump oil through sump oil pump 8, this governing valve is located the pipeline of carrying the sump oil, and the one end and this governing valve of this level gauge are connected, and the other end and the three-phase separator 4 of this level gauge are connected, through the liquid level of sump oil in this level gauge monitoring three-phase separator 4, the flow of carrying the sump oil is adjusted through the governing valve to the liquid level height based on sump oil in the three-phase separator 4. The first transportation pipeline 33 for transporting the other part of the oil phase can also be provided with a liquid level meter and a regulating valve, the regulating valve is positioned on the first transportation pipeline 33, one end of the liquid level meter is connected with the regulating valve, the other end of the liquid level meter is connected with the emptying tower 1, the liquid level of the heavy distillate oil in the emptying tower 1 is monitored through the liquid level meter, and the flow of the other part of the oil phase transported is regulated through the regulating valve based on the liquid level of the heavy distillate oil in the emptying tower 1.
Introduction of the pressure-controlled valve 13: in one possible implementation, the venting system further includes: a pressure-controlled valve 13;
the pressure control valve 13 is positioned on a fourth delivery line, and the fourth delivery line is connected with the Venturi atomization scrubber 5;
a fourth transfer line for transferring steam from the coke drum;
the pressure control valve 13 is used to monitor the pressure of the steam from the coke drum.
In the implementation mode, the pressure of the steam from the coke tower is monitored through the pressure control valve 13, and the phenomenon that the service life of the Venturi atomization scrubber 5, the distributor 6 and the cyclone separator 7 is influenced due to the fact that the impact of the overlarge pressure on the Venturi atomization scrubber 5, the distributor 6 and the cyclone separator 7 is large is avoided.
The emptying system provided by the embodiment of the application comprises an emptying tower 1, a cooling system 2, a circulating system 3, a three-phase separator 4, a venturi atomization scrubber 5 and a distributor 6, wherein a part of oil phase from the circulating system 3 is atomized into first oil phase liquid drops through the venturi atomization scrubber 5, heavy condensed distillate oil in steam from a coke tower is converted into second oil phase liquid drops through the first oil phase liquid drops, coke powder in the steam is collected through the first oil phase liquid drops and the second oil phase liquid drops, the first oil phase liquid drops and the second oil phase liquid drops which are collected with the coke powder are separated from a gas phase in the steam through the distributor 6, the gas phase is cooled through the cooling system 2, and non-condensable gas, water vapor and other oil gases in the gas phase are separated through the three-phase separator 4. The device can separate heavy fraction and fine coke in the steam from gas phase through the venturi atomization scrubber 5 and the distributor 6, so that the gas phase output from the top of the vent tower 1 does not carry the heavy fraction and the fine coke, the separation effect is improved, and the problems of safety and environmental protection, such as blockage of a cooling system 2, standard exceeding of temperature, poor oil-water separation effect and the like caused by gas phase entrainment in a vent system are solved.
Embodiments of the present application provide a method for treating gas phase entrainment, see fig. 3, the method comprising:
step 301: atomizing a part of the oil phase from the circulating system into first oil phase liquid drops through a Venturi atomization scrubber, mixing the first oil phase liquid drops and steam from a coke tower in the Venturi atomization scrubber, and condensing heavy fraction oil in the steam into second oil phase liquid drops through the first oil phase liquid drops.
The oil phase includes first oil phase droplets and second oil phase droplets entrapping coke breeze.
In the step, the oil phase is atomized into first oil phase droplets in a Venturi atomization scrubber by adopting a quenching technology of liquid atomization, the first oil phase droplets are low in temperature and large in specific surface area, and the temperature of heavy distillate oil in steam from a coke tower can be reduced to a condensation temperature to form second oil phase droplets.
Step 302: the coke fines in the steam are captured by the first oil phase droplets and the second oil phase droplets.
And the coke powder in the steam is fully captured by adopting the first oil-phase liquid drops and the second oil-phase liquid drops in the Venturi atomization scrubber through a Venturi dust washing technology, so that the coke powder is separated from the steam.
Step 303: the first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder are separated from the gas phase in the steam through a distributor in the emptying tower.
The gas phase includes non-condensable gases, water vapor and other hydrocarbons.
The mass of oil phase liquid drops trapped with coke powder is continuously increased, and the oil phase liquid drops directly fall into the bottom of the emptying tower after entering the distributor, so that the oil phase liquid drops are separated from the gas phase in the steam.
Step 304: the heavy distillate oil and coke powder carried in the gas phase are further separated by a cyclone separator in the emptying tower.
In the step, a cyclone separator is additionally arranged in the emptying tower, and the oil phase liquid drops trapping the coke powder are separated from the gas phase again through the cyclone separator, so that heavy distillate oil and the coke powder are prevented from being entrained in the gas phase.
Step 305: and outputting the separated gas phase from the top of the emptying tower, and outputting the separated first oil phase liquid drop and the second oil phase liquid drop which are collected with the coke powder from the bottom of the emptying tower as oil phases.
Step 306: the gas phase output from the top of the vent tower is cooled by a cooling system, one part of the oil phase output from the bottom of the vent tower is refluxed to the Venturi atomization scrubber by a circulating system, and the other part is output through a first conveying pipeline.
The cooling system comprises an air cooler and an aftercooler, and the gas phase output from the top of the emptying tower is cooled by the air cooler and then is cooled by the aftercooler.
The circulating system comprises a circulating oil pump and a cooling water tank, the oil phase output from the bottom of the emptying tower is conveyed into the cooling water tank through the circulating oil pump, after the oil phase is cooled in the cooling water tank, one part of the oil phase flows back to the Venturi atomization scrubber to be re-atomized into first oil phase liquid drops, and the other part of the oil phase is output through a first conveying pipeline.
In one possible implementation, the flow rate of the oil phase back into the venturi atomization scrubber can be monitored by a flow meter; monitoring the temperature of the emptying tower through a thermometer; the temperature of the emptying tower is adjusted by changing the flow of the oil phase which flows back to the Venturi atomization scrubber, so that the temperature is favorable for improving the separation effect of the distributor and the cyclone separator.
In the implementation mode, the flow of the oil phase flowing back to the Venturi atomization scrubber is monitored through the flow meter, the feeding temperature is controlled through cascade control of the flow and the feeding temperature, and the gas speed in the emptying tower is controlled.
Step 307: conveying the gas phase cooled by the cooling system to a three-phase separator; the non-condensable gas, the water vapor and other oil gas in the gas phase are separated by a three-phase separator.
Step 308: the separated non-condensable gasses are conveyed by a second conveying line, the separated dirty oil is conveyed by a dirty oil pump, and the separated dirty water is conveyed by a dirty water pump.
The dirty oil comprises other oil gas, and the sewage comprises steam.
In the step, the non-condensable gas conveyed by the second conveying pipeline can be recovered, and can also be combusted by a venting torch. The dirty oil delivered by the dirty oil pump can be delivered into a dirty oil tank or a fractionating tower, and the sewage delivered by the sewage pump can be delivered to a downstream acidic water stripping device.
According to the method for processing the gas phase entrainment, a part of oil phase from a circulating system is atomized into first oil phase liquid drops through a Venturi atomization scrubber, heavy fraction oil in steam from a coke tower is condensed into second oil phase liquid drops through the first oil phase liquid drops, coke powder in the steam is trapped through the first oil phase liquid drops and the second oil phase liquid drops, the first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder are separated from the gas phase in the steam through a distributor, the separated gas phase is output from the top of an emptying tower, and the separated first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder are used as oil phases and are output from the bottom of the emptying tower. According to the method, the heavy fraction and the coke powder in the steam can be separated from the gas phase in the steam through the Venturi atomization scrubber and the distributor, so that the heavy fraction and the coke powder are not carried in the gas phase output from the top of the emptying tower, the separation effect is improved, and the problems of cooling system blockage, over-standard temperature, poor oil-water separation effect and the like caused by gas phase entrainment in an emptying system are solved.
The above description is only for facilitating the understanding of the technical solutions of the present application by those skilled in the art, and is not intended to limit the present application. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (11)
1. A flare system, comprising: the device comprises an emptying tower, a cooling system, a circulating system, a three-phase separator, a Venturi atomization scrubber and a distributor;
one end of the Venturi atomization scrubber is connected with the distributor, and the distributor is positioned in the emptying tower;
the bottom of the emptying tower is connected with one end of the circulating system, and the other end of the circulating system is connected with the other end of the Venturi atomization scrubber;
the top of the emptying tower is connected with one end of the cooling system, and the other end of the cooling system is connected with the first end of the three-phase separator;
the circulating system is used for refluxing a part of oil phase output from the tower bottom of the emptying tower to the Venturi atomization scrubber, and the oil phase comprises first oil phase liquid drops and second oil phase liquid drops, wherein coke powder is trapped in the first oil phase liquid drops and the second oil phase liquid drops;
the venturi atomization scrubber is used for atomizing a part of oil phase from the circulating system into first oil phase liquid drops, condensing heavy fraction oil in steam from a coke tower into second oil phase liquid drops through the first oil phase liquid drops, and trapping coke powder in the steam through the first oil phase liquid drops and the second oil phase liquid drops, wherein the steam comprises noncondensable gas, water vapor and other oil gases besides the heavy fraction oil and the coke powder;
the distributor is used for separating the first oil phase liquid drops and the second oil phase liquid drops which are trapped with coke breeze from the gas phase in the steam, wherein the gas phase comprises the non-condensable gas, the water vapor and the other oil gas;
the cooling system is used for cooling the gas phase output from the top of the emptying tower;
the three-phase separator is used for separating non-condensable gas, water vapor and other oil gas in the gas phase.
2. The venting system of claim 1, further comprising: a cyclone separator;
the cyclone separator is positioned in the emptying tower and above the distributor;
the cyclone separator is used for further separating heavy distillate oil and coke powder carried in the gas phase.
3. The venting system of claim 1, wherein the cooling system comprises: an air cooler and an aftercooler;
one end of the air cooler is connected with the top of the emptying tower, and the other end of the air cooler is connected with one end of the after-cooler;
the other end of the after-cooler is connected with the first end of the three-phase separator.
4. The venting system of claim 1, wherein the circulation system comprises: a circulating oil pump and a cooling water tank;
one end of the circulating oil pump is connected with the bottom of the emptying tower, and the other end of the circulating oil pump is connected with the first end of the cooling water tank;
the second end of the cooling water tank is connected with the other end of the Venturi atomization scrubber, and the third end of the cooling water tank is connected with a first conveying pipeline;
the circulating oil pump is used for conveying an oil phase output from the bottom of the emptying tower to the cooling water tank;
the first transfer line is for outputting another portion of the oil phase.
5. The venting system of claim 1, further comprising: a sump oil pump, a sump pump and a second transfer line;
the second end of the three-phase separator is connected with the sewage pump, the third end of the three-phase separator is connected with the sewage pump, and the fourth end of the three-phase separator is connected with the second conveying pipeline;
the dirty oil pump is used for conveying dirty oil separated by the three-phase separator, and the dirty oil comprises other oil gas;
the sewage pump is used for conveying the sewage separated by the three-phase separator, and the sewage comprises the water vapor;
the second conveying pipeline is used for conveying the non-condensable gas separated by the three-phase separator.
6. The venting system of claim 1, further comprising: flow meters and thermometers;
the circulating system is connected with the Venturi atomization scrubber through a third conveying pipeline, and the flow meter is positioned on the third conveying pipeline;
one end of the thermometer is connected with the flowmeter, and the other end of the thermometer is connected with the emptying tower;
the flow meter is used for monitoring the flow of the oil phase input into the Venturi atomization scrubber from the circulating system;
the thermometer is used for monitoring the temperature of the emptying tower.
7. A method of treating gas phase entrainment, the method comprising:
atomizing a portion of an oil phase from a circulation system into first oil phase droplets by a venturi atomization scrubber, mixing the first oil phase droplets with steam from a coke drum in the venturi atomization scrubber, condensing heavy fraction oil in the steam into second oil phase droplets by the first oil phase droplets, the oil phase comprising first oil phase droplets and second oil phase droplets with trapped coke fines;
capturing the coke fines in the steam by the first oil phase droplets and the second oil phase droplets;
separating the first oil phase liquid drops and the second oil phase liquid drops which are trapped with the coke powder from the gas phase in the steam through a distributor in the emptying tower;
and outputting the separated gas phase from the top of the emptying tower, and outputting the separated first oil phase liquid drop and the second oil phase liquid drop which are collected with the coke powder as oil phases from the bottom of the emptying tower, wherein the gas phase comprises non-condensable gas, water vapor and other oil gases.
8. The method of claim 7, wherein prior to outputting the separated vapor phase from the overhead of the vent column, the method further comprises:
and further separating heavy fraction oil and coke powder carried in the gas phase by a cyclone separator in the emptying tower.
9. The method of claim 7, further comprising:
monitoring the flow rate of the oil phase refluxed into the venturi atomization scrubber by a flow meter;
monitoring the temperature of the evacuation tower by a thermometer;
the temperature of the vent tower is adjusted by varying the flow of oil phase back into the venturi atomization scrubber.
10. The method of claim 7, further comprising:
cooling a gas phase output from the top of the evacuation column by a cooling system;
and refluxing one part of the oil phase output from the bottom of the emptying tower to the Venturi atomization scrubber through the circulating system, and outputting the other part of the oil phase through a first conveying pipeline.
11. The method of claim 10, further comprising:
conveying the gas phase cooled by the cooling system to a three-phase separator;
separating non-condensable gases, water vapor and other oil and gas in the gas phase by the three-phase separator;
the noncondensable gas of separation is carried through the second pipeline, carries the sump oil of separation through the sump oil pump to and carry the sewage of separation through the sump oil pump, include in the sump oil other oil gas, include in the sewage vapor.
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| CN102816582A (en) * | 2012-08-29 | 2012-12-12 | 中国石油天然气股份有限公司 | Method and delayed coking blowdown system for preventing flameout of refinery torch |
| CN104560105A (en) * | 2013-10-29 | 2015-04-29 | 中国石油天然气股份有限公司 | Delayed coking steam evacuating and cooling system and application thereof |
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