CN113462423B - Method for treating gas phase entrainment and venting system - Google Patents
Method for treating gas phase entrainment and venting system Download PDFInfo
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- CN113462423B CN113462423B CN202010247032.7A CN202010247032A CN113462423B CN 113462423 B CN113462423 B CN 113462423B CN 202010247032 A CN202010247032 A CN 202010247032A CN 113462423 B CN113462423 B CN 113462423B
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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
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- 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 an emptying system, and belongs to the technical field of petroleum refining. According to the emptying system provided by the embodiment of the application, part of oil phase from a circulation system is atomized into first oil phase liquid drops through a 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 gas phase in the steam through a distributor. The device can separate heavy fraction and coke powder in steam from gas phase through venturi atomizing washer and distributor, so that heavy fraction and coke powder are not carried in gas phase output from the top of the emptying tower, the separation effect is improved, and the problems of cooling system blockage, temperature exceeding, 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. And more particularly to a method and venting system for treating gas phase entrainment.
Background
In the technical field of petroleum refining, a great amount of steam from a coke tower is generally treated by adopting an emptying system of a delayed coking device, heavy distillate oil and coke powder in the steam are separated from gas by the emptying system and are further respectively recovered, and the steam contains gas phase, heavy distillate oil and coke powder, and the gas phase comprises noncondensable gas, vapor and other oil and gas.
The emptying system in the related art 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 the emptying tower, heavy distillate oil and coke powder are separated from the bottom of the emptying tower after being separated by a baffle in the emptying tower, and the heavy distillate oil and the coke powder flow back to the top of the tower through a circulating system; the gas phase is output from the top of the tower and is separated by a three-phase separator after being cooled by a cooling system.
However, the tray in the emptying tower is easy to fall off in the application process, so that the separation is incomplete, a large amount of heavy distillate oil and coke powder are entrained 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 and an emptying system for treating gas phase entrainment, which can ensure that heavy fraction and coke powder are not carried in a gas phase output from the top of an emptying tower, and improve the separation effect. The specific technical scheme is as follows:
in one aspect, embodiments of the present application provide an evacuation system, the evacuation system including: 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 washer 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 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 which are trapped with coke powder;
the venturi atomizing scrubber is used for atomizing a part of oil phase from the circulating system into first oil phase droplets, condensing heavy fraction oil in steam from a coke tower into second oil phase droplets through the first oil phase droplets, and capturing coke powder in the steam through the first oil phase droplets and the second oil phase droplets, wherein the steam comprises noncondensable gas, water vapor and other oil gas 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 the coke powder 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 noncondensable gas, water vapor and other oil and gas in the gas phase.
In one possible implementation, the venting system further comprises: 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 entrained in the gas phase.
The cooling system includes: an air cooler and a 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 aftercooler;
the other end of the aftercooler 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 washer, and the third end of the cooling water tank is connected with the first conveying pipeline;
the circulating oil pump is used for conveying the 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, the venting system further includes: 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 the dirty oil separated by the three-phase separator, and the dirty oil comprises the other oil gas;
the sewage pump is used for conveying sewage separated by the three-phase separator, and the sewage comprises the water vapor;
the second conveying pipeline is used for conveying the noncondensable gas separated by the three-phase separator.
In another possible implementation, the venting system further includes: a flowmeter and a thermometer;
the circulating system is connected with the Venturi atomization scrubber through a third conveying pipeline, and the flowmeter 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 flowmeter is used for monitoring the flow rate of the oil phase input into the venturi atomizing scrubber from the circulating system;
the thermometer is used for monitoring the temperature of the emptying tower.
In another aspect, embodiments herein provide a method of treating gas phase entrainment, the method comprising:
atomizing a portion of the oil phase from the circulation system into first oil phase droplets by a venturi atomizing scrubber, mixing the first oil phase droplets with steam from a coke drum in the venturi atomizing 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 coke powder trapped therein;
capturing coke powder in the steam through the first oil phase liquid drops and the second oil phase liquid drops;
separating the first oil phase droplets and the second oil phase droplets, in which the coke powder is trapped, from the gas phase in the steam by a distributor in the emptying tower;
outputting the separated gas phase from the top of the emptying tower, taking the separated first oil phase liquid drops and second oil phase liquid drops which are captured with coke powder as oil phases, and outputting the separated gas phase from the bottom of the emptying tower, wherein the gas phase comprises noncondensable gas, water vapor and other oil gases.
In one possible implementation, before the outputting the separated gas phase from the top of the emptying tower, the method further includes:
and further separating heavy distillate oil and coke powder entrained in the gas phase through a cyclone separator in the emptying tower.
In another possible implementation, the method further includes:
monitoring the flow of the oil phase flowing back into the venturi atomizing scrubber by a flow meter;
monitoring the temperature of the emptying tower through a thermometer;
the temperature of the blowdown tower is adjusted by varying the flow rate of the oil phase back to the venturi atomizing scrubber.
In another possible implementation, the method further includes:
cooling the gaseous phase output from the top of the blowdown tower 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, the method further includes:
conveying the gas phase cooled by the cooling system to a three-phase separator;
separating non-condensable gas, water vapor and other oil and gas in the gas phase through the three-phase separator;
the separated non-condensable gas is conveyed through a second conveying pipeline, the separated dirty oil is conveyed through a dirty oil pump, the other oil gas is contained in the dirty oil, and the water vapor is contained in the sewage water.
The beneficial effects that technical scheme that this application embodiment provided brought are:
the embodiment of the application provides a system of blowing out, including the blowing out tower, cooling system, circulation system, three-phase separator, venturi atomizing scrubber and distributor, atomize into first oil phase liquid drop through venturi atomizing scrubber from circulation system's some oil phase, condense into second oil phase liquid drop through first oil phase liquid drop with the heavy fraction oil in the steam that comes from the coke tower, the fine coke in the entrapment steam of through first oil phase liquid drop and second oil phase liquid drop, leave the gaseous phase in first oil phase liquid drop and the second oil phase liquid drop that will trap the fine coke and the steam through the distributor, and then cool off the gaseous phase through cooling system, the noncondensable gas in the separation gaseous phase is through three-phase separator, vapor and other oil gas. The device can separate heavy fraction and coke powder in steam from gas phase through venturi atomizing washer and distributor, so that heavy fraction and coke powder are not carried in gas phase output from the top of the emptying tower, the separation effect is improved, and the problems of cooling system blockage, temperature exceeding, 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 in an embodiment of the present application;
FIG. 2 is a schematic diagram of another venting system provided in an embodiment of the present application;
FIG. 3 is a flow chart of a method of treating vapor phase entrainment provided in an embodiment of the present application.
Reference numerals denote:
1-emptying tower, 2-cooling system, 3-circulating system, 4-three-phase separator, 5-Venturi atomizing scrubber,
6-distributor, 7-cyclone, 8-dirty oil pump, 9-dirty water 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 solution and advantages of the present application more clear, the following embodiments of the present application are described in further detail.
An embodiment of the present application provides an emptying system, referring to fig. 1, the emptying system includes: the system 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;
one end of the Venturi atomization washer 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 the circulating system 3, and the other end of the circulating system 3 is connected with the other end of the Venturi atomization washer 5;
the top of the emptying tower 1 is connected with one end of the cooling system 2, and the other end of the cooling system 2 is connected with the first end of the three-phase separator 4;
the circulation system 3 is used for refluxing a part of the oil phase output from the bottom of the emptying tower 1 to the Venturi atomization washer 5, wherein the oil phase comprises first oil phase liquid drops and second oil phase liquid drops which are trapped with coke powder;
the venturi atomizing washer 5 is used for atomizing a part of oil phase from the circulation system 3 into first oil phase droplets, condensing heavy fraction oil in steam from the coke tower into second oil phase droplets through the first oil phase droplets, and capturing coke powder in the steam through the first oil phase droplets and the second oil phase droplets, wherein the steam comprises noncondensable gas, water vapor and other oil gas 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 noncondensable gas, water vapor and other oil gas in the steam;
the cooling system 2 is used for cooling noncondensable gases, water vapor and other oil gas output from the top of the emptying tower 1;
the three-phase separator 4 is used for separating noncondensable gases, water vapor and other oil and gas.
A multi-layer herringbone or duckbill baffle is arranged in the emptying tower 1 in the related art, and a heat exchange space is provided by the baffle, so that heavy distillate oil and coke powder in steam are condensed. However, in actual production, the baffle falls seriously, which results in the reduction of the separation efficiency of the emptying tower 1 and the reduction of the washing effect of the coke powder, so that a large amount of heavy distillate oil and coke powder enter the top of the emptying tower 1, become a liquid phase with high specific gravity and viscosity when passing through the cooling system 2, and are easy to adhere to the pipe wall, namely wax hanging in production, and then influence the heat exchange effect to cause frequent shutdown and maintenance. The heat exchange effect cannot be ensured due to falling of the baffle, the temperature of the gas phase entering the three-phase separator 4 cannot meet the requirement, and more water vapor can be carried in the non-condensable gas, so that the extinction accident of the emptying torch is caused. 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-water is mixed. In the related art, the sewage separated by the three-phase separator 4 is generally conveyed to an acid water stripping device, dirty oil is conveyed to a dirty oil tank, and when the above situation occurs, the separation effect of the three-phase separator 4 is poor, and pollution is diffused to a tank area and the acid water stripping device. In addition, in the related art, sewage is sometimes conveyed to a cold coke water system for recycling, but due to poor separation effect and excessive sewage, long-term recycling in the cold coke water system can cause accumulation of hydrogen sulfide, serious odor and serious environmental protection problem.
In the embodiment of the application, a quenching technology is adopted in the venturi atomizing scrubber 5 to atomize an oil phase into first oil phase droplets, the oil phase is mainly heavy distillate oil, the first oil phase droplets have larger specific surface area and lower temperature, the first oil phase droplets are fully mixed with steam from a coke tower, cooled and absorbed, the temperature of the heavy distillate oil in the steam is reduced to a condensing temperature to form second oil phase droplets, and the coke powder in the steam is fully trapped by the first oil phase droplets and the second oil phase droplets which are gradually increased through a dust washing technology of a venturi reducing section and a diffusion section in the venturi atomizing scrubber 5. 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 the distributor 6 in the emptying tower 1, and the gas phase comprises noncondensable gas, vapor and other oil gas, so that heavy fractions 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 blockage, exceeding temperature, poor oil-water separation effect and the like of the cooling system 2 caused by gas phase entrainment in the emptying system are solved.
It should be noted that the distributor 6 can further prevent uneven impact of steam and reduce damage to internal parts. In addition, no baffle is arranged in the emptying tower 1 provided by the embodiment of the application.
Introduction of the cyclone 7: in one possible implementation, referring to fig. 2, the venting system further comprises: a cyclone 7;
the cyclone 7 is positioned in the emptying tower 1 and above the distributor 6;
the cyclone 7 is used to further separate the heavy fraction oil and coke breeze entrained in the gas phase.
In the embodiment of the application, the first oil phase liquid drop and the second oil phase liquid drop which are trapped with the coke powder enter the distributor 6 of the emptying tower 1 together with other components in the steam, and in the distributor 6, the larger oil phase liquid drop directly falls into the bottom of the emptying tower 1, and the smaller oil phase liquid drop possibly ascends along with the gas phase in the steam, so that heavy distillate oil and the coke powder are entrained in the gas phase. In the implementation mode, the cyclone 7 is additionally arranged in the emptying tower 1, and small oil phase liquid drops are separated from gas phases in steam again through the cyclone 7, so that the gas phases output from the tower top are clean, heavy distillate oil and coke powder are not carried, and the problems of blockage of a cooling system 2, temperature exceeding, poor oil-water separation effect and the like caused by gas phase entrainment in the emptying system are solved.
The cyclone separator 7 provided by the embodiment of the application can achieve separation efficiency of more than 99%, and achieves no entrainment of gas phase at the top of the tower.
The distance between the cyclone 7 and the distributor 6 may be set and changed as required, and in the embodiment of the present application, this is not particularly limited.
Introduction of the 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 the first end of the three-phase separator 4.
In this implementation, the gas phase output from the top of the emptying tower 1 is cooled by the air cooler 21, then condensed and cooled by the aftercooler 22, and then the cooled gas phase is input into the three-phase separator 4 for further separation, wherein the gas phase comprises noncondensable gas, vapor and other oil gas.
In this implementation, the air cooler 21 uses ambient air as a cooling medium, and the air cooler 21 initially cools and cools the gas phase, and then the aftercooler 22 further cools the gas phase. The aftercooler 22 has small volume, small pitch, very uniform temperature distribution and good cooling effect.
Introduction of 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 a 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 a cooling water tank 32;
the second end of the cooling water tank 32 is connected with the other end of the Venturi atomization washer 5, and the third end of the cooling water tank 32 is connected with the 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 portion of the oil phase.
In this embodiment, the oil phase outputted from the bottom of the emptying tower 1, which mainly includes heavy fraction oil, is outputted to the cooling water tank 32 by the circulation oil pump 31, and after being cooled in the cooling water tank 32, a part of the oil phase is outputted to the venturi atomizing scrubber 5, and the part of the oil phase is atomized again into oil phase droplets by the venturi atomizing scrubber 5, and the other part of the oil phase is outputted through the first transfer line 33.
In one possible implementation, this further portion of the oil phase may be conveyed into the dirty oil tank via the first conveying line 33; in another possible implementation, it can also be fed into the fractionation column via the first feed line 33 for reprocessing. In the embodiment 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 venting system further comprises: a sump 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 sewage separated by the three-phase separator 4, and the sewage comprises water vapor;
the second transfer line 10 is used for transferring the noncondensable 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 output. The form of the three-phase separator 4 may be set and modified as needed, and in the embodiment of the present application, this is not particularly limited, and the three-phase separator 4 is, for example, 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 dirty oil is output from the second end of the three-phase separator 4 and is conveyed by the dirty 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 noncondensable gases are conveyed via a second conveying line 10.
In one possible implementation, the dirty oil conveyed by the dirty oil pump 8 may be input to a dirty oil tank or a fractionating tower together with another part of the oil phase output from the cooling water tank 32, the sewage conveyed by the dirty water pump 9 may be input to the acid water stripping device through a conveying pipeline for treatment, and the noncondensable gas conveyed by the second conveying pipeline 10 may be recovered, or may be discharged after being combusted through the emptying torch, thereby avoiding environmental pollution.
It should be noted that, the emptying system provided by the embodiment of the application can fundamentally solve the problem of gas phase entrainment, and the heavy distillate oil and coke powder do not enter the top of the tower any more, so that the operation of the cooling system 2 is ensured. The steam speed entering the emptying tower 1 is greatly reduced, the impact on the distributor 6 and the cyclone 7 in the tower is small, and the internal parts are stable and do not fall off any more. The three-phase separator 4 has good oil, gas and water separation effect, and the sulfur-containing sewage can be directly conveyed to the acid water stripping device without being discharged in an open mode, thereby meeting the requirements of the current environmental protection policy and regulation. And the temperature of the three-phase separator 4 is low, the water content in the noncondensable gas is low, and the recovery or emptying of the torch is safer. And can also meet the requirement of long-period operation of the oil refining device.
Introduction of flow meter 11 and thermometer 12: in one possible implementation, the venting system further comprises: a flow meter 11 and a thermometer 12;
the circulating system 3 and the Venturi atomization washer 5 are connected through a third conveying pipeline, and a flowmeter 11 is positioned on the third conveying pipeline;
one end of a thermometer 12 is connected with a flowmeter 11, and the other end of the thermometer 12 is connected with a vent tower 1;
the flow meter 11 is used for monitoring the flow rate of the oil phase input into the venturi atomizing scrubber 5 from the circulation system 3;
the thermometer 12 is used to monitor the temperature of the vent tower 1.
In this implementation, the flow rate of the oil phase input into the venturi atomizing scrubber 5 is monitored by the flow meter 11, the temperature in the blowdown tower 1 is monitored by the thermometer 12, and the temperature in the blowdown 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 large, the temperature of the emptying tower 1 is low; when the flow rate of the oil phase is small, the temperature of the vent column 1 is high. When the temperature in the emptying tower 1 is lower, the separation of heavy fraction and coke powder from 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 one possible implementation, a thermometer 12 may also be provided in the line from the top of the vent column 1 for outputting the gas phase, the temperature of which is monitored by the thermometer 12.
In another possible implementation, a liquid level meter and a regulating valve are arranged on the pipeline for conveying sewage through the sewage pump 9, the regulating valve is arranged 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 the sewage in the three-phase separator 4 is monitored through the liquid level meter, and the flow rate of the sewage is regulated through the regulating valve based on the liquid level of the sewage in the three-phase separator 4. The pipeline for conveying the dirty oil through the dirty oil pump 8 can also be provided with a liquid level meter and a regulating valve, wherein the regulating valve is positioned on the pipeline for conveying the dirty oil, 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 the dirty oil in the three-phase separator 4 is monitored through the liquid level meter, and the flow of the dirty oil is regulated through the regulating valve based on the liquid level of the dirty oil in the three-phase separator 4. The first conveying pipeline 33 for conveying another part of oil phase can also be provided with a liquid level meter and a regulating valve, wherein the regulating valve is positioned on the first conveying 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 heavy fraction oil in the emptying tower 1 is monitored through the liquid level meter, and the flow rate of the conveyed another part of oil phase is regulated through the regulating valve based on the liquid level of the heavy fraction oil in the emptying tower 1.
Introduction of the pressure control valve 13: in one possible implementation, the venting system further comprises: a pressure-controlled valve 13;
the pressure control valve 13 is positioned on a fourth conveying pipeline which 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 vapor from the coke drum.
In this implementation, the pressure of the steam from the coke drum is monitored by the pressure control valve 13, so that the impact of the excessive pressure on the venturi atomizing scrubber 5, the distributor 6 and the cyclone 7 is avoided, and the service lives of the venturi atomizing scrubber 5, the distributor 6 and the cyclone 7 are influenced.
The embodiment of the application provides a system of blowing out, including blowing out tower 1, cooling system 2, circulation system 3, three-phase separator 4, venturi atomizing scrubber 5 and distributor 6, atomize into first oil phase liquid drop through venturi atomizing scrubber 5 from the partly oil phase of circulation system 3, condense into the second oil phase liquid drop through first oil phase liquid drop with the heavy fraction oil in the steam that comes from the coke tower, the coke powder in the entrapment steam of through first oil phase liquid drop and second oil phase liquid drop, leave the gaseous phase in the first oil phase liquid drop and the second oil phase liquid drop that will trap the coke powder and the steam through distributor 6, and then cool off the gaseous phase through cooling system 2, separate noncondensable gas in the gaseous phase, vapor and other oil gas through three-phase separator 4. The device can separate heavy fraction and coke powder in steam from gas phase through venturi atomizing washer 5 and distributor 6, so that heavy fraction and 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 blockage of cooling system 2, temperature exceeding, poor oil-water separation effect and the like caused by gas phase entrainment in the emptying system are solved.
Embodiments of the present application provide a method of treating gas phase entrainment, see fig. 3, comprising:
step 301: atomizing a portion of the oil phase from the circulation system into first oil phase droplets by a venturi atomizing scrubber, mixing the first oil phase droplets with steam from the coke drum in the venturi atomizing scrubber, condensing heavy fraction oil in the steam into second oil phase droplets by the first oil phase droplets.
The oil phase includes first oil phase droplets and second oil phase droplets that trap coke powder.
In the step, a quenching technology of liquid atomization is adopted in a Venturi atomization washer to atomize the oil phase into first oil phase liquid drops, the temperature of the first oil phase liquid drops is lower, the first oil phase liquid drops have larger specific surface area, and the temperature of heavy distillate oil from coke tower steam can be reduced to a condensation temperature to form second oil phase liquid drops.
Step 302: coke powder in the steam is captured by the first oil phase droplets and the second oil phase droplets.
And fully trapping the coke powder in the steam by adopting first oil phase liquid drops and second oil phase liquid drops through a Venturi dust washing technology in a Venturi atomization scrubber, so that the coke powder is separated from the steam.
Step 303: the first oil phase droplets and the second oil phase droplets, which are trapped with coke powder, are separated from the gas phase in the steam by a distributor in the emptying tower.
The gas phase includes noncondensable gases, water vapor and other hydrocarbons.
The mass of the oil phase liquid drops with the coke powder is continuously increased, and the oil phase liquid drops directly fall into the bottom of the emptying tower after entering the distributor, thereby being separated from the gas phase in the steam.
Step 304: and further separating heavy distillate oil and coke powder carried in the gas phase 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 with the coke powder trapped therein 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: outputting the separated gas phase from the top of the emptying tower, taking the separated first oil phase liquid drops and second oil phase liquid drops which are captured with coke powder as oil phases, and outputting from the bottom of the emptying tower.
Step 306: the gas phase output from the top of the vent tower is cooled by a cooling system, a part of the oil phase output from the bottom of the vent tower is refluxed to the venturi atomizing scrubber by a circulating system, and the other part is output by 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 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 being cooled in the cooling water tank, one part of the oil phase is returned into the Venturi atomizing washer to be atomized again 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 of the oil phase back into the venturi atomizing scrubber may be monitored by a flow meter; monitoring the temperature of the emptying tower through a thermometer; the temperature of the vent tower is regulated by changing the flow of the oil phase flowing back into the Venturi atomization scrubber, so that the temperature is beneficial to improving the separation effect of the distributor and the cyclone.
In the implementation mode, the flow rate of the oil phase flowing back into the Venturi atomization scrubber is monitored through the flowmeter, cascade control is carried out through the flow rate and the feeding temperature, the feeding temperature is guaranteed to be controllable, and the air speed in the emptying tower is controllable.
Step 307: conveying the gas phase cooled by the cooling system to a three-phase separator; noncondensable gas, vapor and other oil and gas in the gas phase are separated by a three-phase separator.
Step 308: the separated non-condensable gas is conveyed through the second conveying pipeline, the separated dirty oil is conveyed through the dirty oil pump, and the separated sewage is conveyed through the dirty water pump.
The dirty oil comprises other oil gas, and the sewage comprises water vapor.
In this step, the noncondensable gas conveyed through the second conveying line can be recovered or can be burned through a flare. The dirty oil delivered by the dirty oil pump may be delivered to a dirty oil tank or to a fractionation column, and the dirty water delivered by the dirty water pump may be delivered to a downstream sour water stripper.
According to the method for treating gas phase entrainment, a part of oil phase from a circulation system is atomized into first oil phase droplets through a Venturi atomization scrubber, heavy fraction oil in steam from a coke tower is condensed into second oil phase droplets through the first oil phase droplets, coke powder in the steam is trapped through the first oil phase droplets and the second oil phase droplets, the first oil phase droplets and the second oil phase droplets which are trapped with the coke powder are separated from gas phase in the steam through a distributor, the separated gas phase is output from the top of an emptying tower, the separated first oil phase droplets and the separated second oil phase droplets which are trapped with the coke powder are used as oil phases, and the separated first oil phase droplets and the separated second oil phase droplets are output from the bottom of the emptying tower. According to the method, the venturi atomizing washer and the distributor can separate heavy fraction and coke powder in steam from gas phase in the steam, 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, temperature exceeding, poor oil-water separation effect and the like caused by gas phase entrainment in the emptying system are solved.
The foregoing is merely for facilitating 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, etc. made within the spirit and principles of the present application should be included in the protection scope of the present application.
Claims (8)
1. An evacuation system, the evacuation system comprising: the device comprises an emptying tower, a cooling system, a circulating system, a three-phase separator, a Venturi atomization scrubber, a distributor, a cyclone separator and a pressure control valve;
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 one end of the Venturi atomization washer, the other end of the Venturi atomization washer is connected with the distributor, the distributor and the cyclone are both positioned in the emptying tower, and the cyclone is positioned above the distributor;
the third end of the cooling water tank is connected with the first conveying pipeline;
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 pressure control valve is positioned on a fourth conveying pipeline, and the fourth conveying pipeline is connected with the Venturi atomization scrubber;
the circulating oil pump is used for conveying the oil phase output from the bottom of the emptying tower to the cooling water tank;
the cooling water tank is used for cooling the oil phase, and after cooling, outputting a part of the oil phase to the Venturi atomization scrubber; the oil phase comprises first oil phase liquid drops and second oil phase liquid drops which are trapped with coke powder;
the first conveying pipeline is used for conveying the other part of the oil phase into a dirty oil tank or a fractionating tower for recycling;
the venturi atomizing scrubber is used for atomizing a part of oil phase from the cooling water tank into first oil phase droplets, condensing heavy fraction oil in steam from the coke tower conveyed through the fourth conveying pipeline into second oil phase droplets through the first oil phase droplets, and capturing coke powder in the steam through the first oil phase droplets and the second oil phase droplets, wherein the steam comprises noncondensable gas, water vapor and other oil gas besides the heavy fraction oil and the coke powder;
the pressure control valve is used for controlling the pressure of steam from the coke tower and stabilizing the steam flow;
the distributor 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 the gas phase in the steam, wherein the gas phase comprises the non-condensable gas, the water vapor and the other oil gas;
the cyclone separator is used for further separating heavy distillate oil and coke powder entrained in the gas phase;
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 noncondensable gas, water vapor and other oil and gas in the gas phase.
2. The venting system of claim 1, wherein the cooling system comprises: an air cooler and a 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 aftercooler;
the other end of the aftercooler is connected with the first end of the three-phase separator.
3. The venting system of claim 1, further comprising: 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 the dirty oil separated by the three-phase separator, and the dirty oil comprises the other oil gas;
the sewage pump is used for conveying sewage separated by the three-phase separator, and the sewage comprises the water vapor;
the second conveying pipeline is used for conveying the noncondensable gas separated by the three-phase separator.
4. The venting system of claim 1, further comprising: a flowmeter and a thermometer;
the cooling water tank is connected with the Venturi atomization scrubber through a third conveying pipeline, and the flowmeter 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 flowmeter is used for monitoring the flow rate of the oil phase input into the venturi atomizing scrubber from the circulating system;
the thermometer is used for monitoring the temperature of the emptying tower.
5. A method of treating gas phase entrainment, the method comprising:
controlling the pressure of steam from the coke tower through a pressure control valve, and stabilizing the steam flow;
conveying the oil phase output from the bottom of the emptying tower to a cooling water tank through a circulating oil pump;
cooling the oil phase through the cooling water tank, and outputting a part of the oil phase to a Venturi atomization scrubber after cooling;
conveying the other part of the oil phase into a dirty oil tank or a fractionating tower through a first conveying pipeline for recycling;
atomizing a portion of the oil phase from the cooling water tank into first oil phase droplets by the venturi atomizing scrubber, mixing the first oil phase droplets and the steam in the venturi atomizing 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 coke powder trapped therein;
capturing coke powder in the steam through the first oil phase liquid drops and the second oil phase liquid drops;
separating the first oil phase droplets and the second oil phase droplets, in which the coke powder is trapped, from the gas phase in the steam by a distributor in the emptying tower;
further separating heavy distillate oil and coke powder entrained in the gas phase by a cyclone separator in the emptying tower;
outputting the separated gas phase from the top of the emptying tower, taking the separated first oil phase liquid drops and second oil phase liquid drops which are captured with coke powder as oil phases, and outputting the separated gas phase from the bottom of the emptying tower, wherein the gas phase comprises noncondensable gas, water vapor and other oil gases.
6. The method of claim 5, wherein the method further comprises:
monitoring the flow of the oil phase flowing back into the venturi atomizing scrubber by a flow meter;
monitoring the temperature of the emptying tower through a thermometer;
the temperature of the blowdown tower is adjusted by varying the flow rate of the oil phase back to the venturi atomizing scrubber.
7. The method of claim 5, wherein the method further comprises:
the gaseous phase output from the top of the blowdown tower is cooled by a cooling system.
8. The method of claim 7, wherein the method further comprises:
conveying the gas phase cooled by the cooling system to a three-phase separator;
separating non-condensable gas, water vapor and other oil and gas in the gas phase through the three-phase separator;
the separated non-condensable gas is conveyed through a second conveying pipeline, the separated dirty oil is conveyed through a dirty oil pump, the other oil gas is contained in the dirty oil, and the water vapor is contained in the sewage water.
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| CN104560105A (en) * | 2013-10-29 | 2015-04-29 | 中国石油天然气股份有限公司 | Delayed coking steam blowing and emptying cooling system and application thereof |
| CN105132041A (en) * | 2015-08-13 | 2015-12-09 | 王树宽 | Liquid-phase dust removing system and liquid-phase dust removing method of pyrolysis coke-oven gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102816582A (en) * | 2012-08-29 | 2012-12-12 | 中国石油天然气股份有限公司 | Method for preventing refinery torch from flameout and delayed coking emptying system |
| CN104560105A (en) * | 2013-10-29 | 2015-04-29 | 中国石油天然气股份有限公司 | Delayed coking steam blowing and emptying cooling system and application thereof |
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