CN112999815B - Device and method for heat exchange washing of oil gas - Google Patents
Device and method for heat exchange washing of oil gas Download PDFInfo
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- CN112999815B CN112999815B CN202110289444.1A CN202110289444A CN112999815B CN 112999815 B CN112999815 B CN 112999815B CN 202110289444 A CN202110289444 A CN 202110289444A CN 112999815 B CN112999815 B CN 112999815B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
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- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
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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
- B01D53/14—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 absorption
- B01D53/1487—Removing organic compounds
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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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/21—Mixing gases with liquids by introducing liquids into gaseous media
- B01F23/213—Mixing gases with liquids by introducing liquids into gaseous media by spraying or atomising of the liquids
- B01F23/2132—Mixing gases with liquids by introducing liquids into gaseous media by spraying or atomising of the liquids using nozzles
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/90—Heating or cooling systems
- B01F35/91—Heating or cooling systems using gas or liquid injected into the material, e.g. using liquefied carbon dioxide or steam
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Abstract
The invention provides a device and a method for oil gas heat exchange washing, wherein the device comprises: the oil-gas heat exchange washing tank comprises an oil-gas inlet, a wax oil spray pipe, an oil-gas outlet, an inner cylinder, a heat exchange spray head, a washing spray head, a rotational flow plate, a tank body and a circulating oil outlet. The method comprises the following steps: the oil gas at the top of the tower is subjected to mixing, cooling heat exchange, washing and coke deposition, gas-liquid separation and other process treatments, and most coke powder in the oil gas at the top of the tower is washed into the circulating oil, so that the coke powder content entering the fractionating tower is reduced. After the circulating oil is filtered to remove the carried coke powder, one part of the circulating oil returns to the washing spray head to continuously wash the oil gas, and the other part of the circulating oil flows into the fractionating tower to enter the circulation again. The invention can effectively reduce the coke powder amount entering the fractionating tower along with the oil gas, thereby improving the product quality of the delayed coking device, prolonging the operation period of the delayed coking device and the downstream devices and saving the operation cost.
Description
Technical Field
The invention relates to a delayed coking technology in the field of petroleum refining, in particular to a device and a method for oil gas heat exchange washing, and more particularly, the device is used for carrying out mixing, cooling heat exchange, washing and coke deposition, gas-liquid separation and other process treatments on oil gas at the top of a tower, washing most coke powder in the oil gas at the top of the tower to circulating oil, and thus reducing the coke powder content of the oil gas entering a fractionating tower.
Background
The delayed coking process has the advantages of good adaptability to raw materials, thorough decarburization, low equipment investment and operation cost and the like, and is an important means for processing heavy and poor crude oil in refineries at present. In terms of the production characteristics, the process is a continuous production and discontinuous operation process. Two coke drums are used as a group, when one coke drum is in an online coking state, the other coke drum is subjected to operations such as coke cooling and decoking, and continuous production is realized through the alternate operation of the two coke drums.
Along with the coke formation state, coke is accumulated in the coke tower to lead to the gradual rise of the material level, and when the material level is too high or the oil gas foaming phenomenon is serious, coke powder can be taken away from the tower top by the oil gas. Secondly, in the process of blowing steam to cool coke in the coke tower, the steam with a certain speed can also carry coke powder into the fractionating tower at a high material level. After entering a fractionating tower, the coke powder is easy to bond with organic macromolecular compounds generated in the polymerization reaction process of unsaturated hydrocarbons such as alkadiene and the like, so that coke particles grow gradually, and equipment is blocked by precipitation, coking and coking; the heat exchanger is easy to be scaled and blocked, the heat exchange effect is influenced, even shutdown and cleaning are needed, and the long-period operation of the device is seriously influenced; when the distillate oil enters a downstream gasoline hydrogenation device and the like, the distillate oil is deposited on the surface of a catalyst, so that the pressure drop of a reactor bed layer is increased, the catalyst is inactivated and the like. Therefore, on the basis of ensuring the crude oil feedstock properties, setting the throughput in accordance with the facility apparatus performance, and effectively controlling the outlet temperature of the heating furnace, it is also necessary to stop the feeding when the stock level reaches two thirds of the height of the coke drum, and to switch the coke drum. However, the oil gas still inevitably carries coke powder to enter the fractionating tower, so that special equipment is further arranged before the oil gas at the top of the tower enters the fractionating tower to remove the coke powder in the oil gas.
Chinese utility model patent (CN208762454U) discloses a slow down device of coke tower top export oil gas pipeline coking, through set up into tower rapid cooling oil pipe line in vertical big oil gas pipeline, the interval sets up a plurality of shower nozzles on the outer fringe face of income tower rapid cooling oil pipe line, shower nozzle spun liquid drop outline line covers in the coke tower oil gas pipeline and the crossing looks of coke tower below region, spray regime covers this regional coke tower oil gas pipeline entry, with oil gas contact, cooling and washing, can slow down the coking of top of the tower oil gas export pipeline, the extension delays coking device's start-up cycle etc. nevertheless because pipeline contact distance is short, and a large amount of atomizing oil drips and high temperature oil gas contact after, can not play the decoking effect because of endothermic gasification.
The Chinese invention patent (CN106244189A) discloses an ash-containing high-temperature oil-gas washing and separating device and a washing and separating method, which comprise a washing tower, wherein the side wall of the washing tower is connected with a washing and scrubbing gas leading-in pipe; the device is characterized in that the lower part of the washing tower is a washing area, the middle part of the washing tower is a cooling area, and the upper part of the washing tower is an oil-gas separation area; the outlet of the tower top of the washing tower is connected with a light oil gas discharge pipeline, the light oil gas discharge pipeline is connected with the inlet of the condensation separator, and the liquid phase outlet of the condensation separator is simultaneously connected with a light oil circulating pipeline and a light oil recovery pipeline; the outlet of the light oil circulating pipeline is connected with a first spraying device; the tower bottom outlet of the washing tower is connected with a second spraying device through a heavy oil circulating pipeline; a cooler, a heavy oil filter and an oil pump are arranged on the heavy oil circulating pipeline; the first spraying device and the second spraying device are arranged in the cooling area, and the first spraying device is positioned above the second spraying device; the inlet pipe extends into the lower part of the washing zone. The device has good decoking effect, energy conservation and low consumption, is not easy to cause equipment blockage, but the route from the first spraying device to the oil-gas outlet is too short, and the oil-gas carries a certain amount of washing oil only by removing the washing oil by a condensation separator.
Therefore, it is necessary to design a method and a device for oil and gas to be fully contacted for heat absorption, washing and decoking and gas-liquid separation.
Disclosure of Invention
The invention provides a device and a method for heat exchange washing of oil gas, which can effectively reduce the coke powder amount entering a fractionating tower along with oil gas, thereby improving the product quality of a delayed coking device and prolonging the operation period of the delayed coking device and downstream devices.
One of the purposes of the invention is to provide a device for heat exchange and washing of oil gas:
the oil-gas heat exchange washing tank comprises an oil-gas inlet, a wax oil spray pipe, an oil-gas outlet, an inner cylinder, a heat exchange spray head, a washing spray head, a rotational flow plate, a tank body and a circulating oil outlet.
The oil-gas heat exchange washing tank 12 is arranged behind a coking tower, the upper part of the oil-gas heat exchange washing tank 12 is provided with a wax oil spray pipe 3 wrapping an oil-gas spray pipe 4, an oil-gas inlet 1 is arranged at the top of the oil-gas spray pipe 4, a wax oil inlet 2 is positioned at the upper part of the column section of the wax oil spray pipe 3, the lower outlet of the wax oil spray pipe 3 is connected with an inner cylinder 6, a hot spray head 7 and a washing spray head 8 are arranged in the inner cylinder 6 from top to bottom in a replacement manner, a rotational flow plate 9 is arranged at the bottom of the inner cylinder 6, the tank body 10 is a vertical pressure container, a circulating oil outlet 11 is arranged at the bottom of the tank body 10, and an oil-gas outlet 5 is arranged at the conical section of the tank body 10;
the tower top oil gas pipeline 18 is connected with the oil gas inlet 1, and a flowmeter 14-1 is arranged on the pipeline; the cooling wax oil pipeline 19 from the fractionating tower is provided with two branch pipelines, one branch pipeline is a wax oil spraying and mixing pipeline 20 connected with a wax oil inlet 2, an automatic regulating valve 17-1 is arranged on the pipeline, the other branch pipeline is a heat exchange wax oil pipeline 21 connected with a heat exchange spray head 7, and the pipeline is provided with the automatic regulating valve 17-2; the circulating oil outlet 11 is connected with a circulating oil pipeline 23 through a filter 13, an automatic regulating valve 17-4 is arranged on the pipeline, a branch pipeline at the downstream of the filter 13 is a washing circulating oil pipeline 22, the washing circulating oil pipeline 22 is connected with a washing spray head 8, an automatic regulating valve 17-3 and a flowmeter 14-2 are arranged on the pipeline, an oil gas outlet 5 and an oil gas outlet pipeline 24 are connected to a fractionating tower, a thermometer 16 is arranged on the pipeline, and a liquid level meter 15 is arranged at the lower part of the tank body 10.
In a preferred embodiment, the upper part of the wax oil spray pipe is conical, and the included angle between the conical surface and the central axis is 37-52 degrees. The lower parts of the oil gas spray pipe and the wax oil spray pipe are designed to be conical, and the included angle between the conical surface and the central axis is 24-37 degrees.
In another preferred embodiment, the heat exchange spray head and the washing spray head are nozzle distributors, the distance between the heat exchange spray head and the outlet of the spray pipe is 0.1-0.18 of the length of the tank, and the distance between the washing spray head and the heat exchange spray head is 0.07-0.12 of the length of the tank.
In another preferred embodiment, the cyclone plate is connected with the bottom of the inner barrel, the distance from the washing spray head is 0.12-0.2 of the length of the tank body, and the thickness of the cyclone plate is 0.02-0.05 of the length of the tank body.
In another preferred embodiment, the ratio of the diameter of the can body to the inner barrel is 1.2 to 1.5.
The second purpose of the invention is to provide a method for oil gas heat exchange washing, which comprises the following steps:
(a) the oil gas at the top of the coke tower and the oil gas spraying wax mixing oil respectively enter an oil gas heat exchange washing tank 12 from an oil gas inlet 1 and a wax oil inlet 2, so that the oil gas at the top of the coke tower and the oil gas spraying wax mixing oil are fully mixed in an inner cylinder 6 to obtain mixed oil gas. The oil-gas spraying mixed wax oil in the oil-gas spray pipe 3 is used for shunting the cooling wax oil of the fractionating tower, the feeding flow of the oil-gas spraying mixed wax oil is adjusted by a flowmeter 14-1 through an automatic adjusting valve 17-1 according to the flow of the tower top oil gas, and the cooling wax oil of the fractionating tower is used for shunting the wax oil distilled by the fractionating tower;
(b) and (b) contacting the mixed oil gas obtained in the step (a) with atomized oil gas heat exchange wax oil sprayed by a heat exchange spray head 7 for heat exchange. Oil-gas heat exchange wax oil is divided for cooling wax oil of the fractionating tower, and the oil-gas heat exchange wax oil feeding flow is adjusted by a thermometer 16 through an automatic adjusting valve 17-2 according to the temperature of oil gas subjected to heat exchange washing and heading to the fractionating tower;
(c) and (c) flushing and washing the mixed oil gas subjected to heat exchange in the step (b) with atomized washing circulating oil sprayed by a washing nozzle 8. The washing circulating oil is divided into circulating oil after being decoked by the filter 13, and the feeding flow of the washing circulating oil is adjusted by the flowmeter 14-2 through the automatic adjusting valve 17-3 according to the flow per se;
(d) carrying out gas-liquid two-phase efficient cyclone separation on the mixed oil gas washed in the step (c) through a cyclone plate 9;
(e) and (d) allowing oil gas subjected to gas-liquid separation in the step (d) to flow to a fractionating tower through an oil gas outlet 5 of a conical section of a tank body 10 after gravity settling, allowing circulating oil containing coke powder to settle to the bottom of the tank body 10, removing the coke powder from a circulating oil outlet 11 through a filter 13, allowing one part of the circulating oil to flow to a washing spray head 8, and allowing the other part of the circulating oil to flow to the fractionating tower. The flow rate of the circulating oil is adjusted by a liquid level meter 15 through an automatic adjusting valve 17-4 according to the liquid level in the tank.
In a preferred embodiment, the method further comprises the steps of: in the step (a), the temperature of the oil gas at the top of the oil gas inlet 1 is 380-420 ℃, and the flow ratio of the oil gas at the top of the tower to the oil gas spraying wax oil is 0.3-0.7.
In another preferred embodiment, in step (b), the heat exchange nozzle 7 atomizes liquid droplets with a diameter of 0.5-1mm, an average particle diameter of 0.7-0.8mm, and the heat exchange circulating oil flow rate is 0.8-1.2 of the oil gas flow rate.
In another preferred embodiment, in step (c), the diameter of the atomized liquid droplets of the washing nozzle 8 is 0.6 to 1.2mm, the average particle diameter is 0.8 to 0.9mm, and the washing circulation oil flow rate is 1.3 to 1.8 of the oil gas flow rate.
In another preferred embodiment, in step (e), the wax oil level in the oil-gas heat exchange washing tank 12 is not higher than 90% of the height from the bottom of the tank body 10 to the bottom of the cyclone plate 9, and the temperature of the oil gas after the oil-gas flows out of the conical section of the tank body 10 and is 370-400 ℃.
The effective benefits are as follows:
the method and the device have the main advantages that:
(1) the processes of mixing, heat exchange, washing, centrifugal separation and gravity settling of the invention realize the mixed mass transfer of oil gas and wax oil, and promote the enrichment of coke powder and heavy oil components in the oil gas into the wax oil. Meanwhile, the upper part of the wax oil spray pipe 3 is conical, so that the dead zone is eliminated; the lower parts of the wax oil spray pipe 3 and the oil gas spray pipe 4 are designed to be conical, so that the effect of increasing the flow velocity of an outlet and strengthening mixing is achieved; the spraying directions of the heat exchange spray head 7 and the washing spray head 8 are opposite to the flowing direction of the mixed oil gas, the gas velocity of the mixed oil gas is effectively reduced by the reverse mixing effect, and the full heat exchange and washing of the oil gas are facilitated; the mixed oil gas is subjected to gas-liquid separation by the cyclone plate 9 and then is subjected to gravity settling, the oil phase carries coke powder for settling, and the gas phase flows to the fractionating tower from the oil gas outlet 5 at the upper part of the tank body 10, so that the secondary entrainment is obviously reduced compared with the situation of only adopting a centrifugal separation structure.
(2) The device for oil gas heat exchange and washing is placed behind a coking tower and in front of a fractionating tower to deeply decoke oil gas on the top of the tower, and has the advantages of compact structure and small occupied area. In addition, the wax oil carrying the coke powder is recycled after being decoked by the filter 13, thereby achieving better economic benefit.
(3) The method and the device are suitable for heat exchange washing of the delayed coking quenching oil gas, are also suitable for devices for removing harmful substances in the gas and the like, and are suitable for great popularization in the petrochemical industry.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification to further illustrate the invention and not limit the invention.
FIG. 1 is a schematic cross-sectional view of an oil-gas heat exchange washing device and internals according to a preferred embodiment of the present invention.
Wherein the reference numerals denote the following devices and internals:
1: oil gas inlet
2: wax oil inlet
3: wax oil spray pipe
4: oil gas spray pipe
5: oil gas outlet
6: inner barrel
7: heat exchange spray head
8: washing spray head
9: rotational flow plate
10: tank body
11: outlet for circulating oil
12: oil gas heat exchange washing tank
13: filter
14-1 and 14-2: flow meter
15: liquid level meter
16: temperature meter
17-1, 17-2, 17-3 and 17-4: automatic regulating valve
18: tower top oil gas pipeline
19: cooling wax oil pipeline
20: wax oil spraying and mixing pipeline
21: heat exchange wax oil pipeline
22: washing circulating oil pipeline
23: circulating oil pipeline
24: oil gas outlet pipeline
Detailed Description
In order to make the technical problems, technical solutions and advantageous effects solved by the present invention more clearly apparent, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
After extensive and intensive research, the inventor of the application finds that the defects of poor decoking effect, secondary entrainment and the like in the existing decoking process can be effectively overcome through processes such as efficient mixing, contact heat exchange, opposite flushing washing, centrifugal separation, gravity settling and the like; meanwhile, the whole heat exchange washing device is placed behind the coking tower and in front of the fractionating tower to deeply decoke oil gas on the top of the tower, the equipment structure is compact, the occupied area is small, and the modification cost is reduced. In addition, the wax oil carrying the coke powder is recycled after being decoked by the filter 13, thereby achieving better economic benefit. The present invention has been completed based on the above conception and finding.
Figure 1 is a schematic cross-sectional view of an oil-gas heat exchange washing device and internals according to a preferred embodiment of the present invention. The oil-gas heat exchange washing tank is arranged behind the coking tower, a wax oil spray pipe wraps an oil-gas spray pipe at the upper part of the oil-gas heat exchange washing tank, an oil-gas inlet is formed in the top of the oil-gas spray pipe and is positioned at the upper part of a column section of the wax oil spray pipe, an outlet at the lower part of the wax oil spray pipe is connected with an inner cylinder, a hot spray head and a washing spray head are arranged in the inner cylinder from top to bottom in a replaceable manner, a rotational flow plate is arranged at the bottom of the inner cylinder, the tank body is a vertical pressure container, an oil-gas outlet is formed in a conical section of the tank body, and a circulating oil outlet is formed in the bottom of the tank body;
the tower top oil gas pipeline is connected with an oil gas inlet, and a flowmeter is arranged on the pipeline; the cooling wax oil pipeline from the fractionating tower is provided with two branch pipelines, one branch pipeline is a wax oil spraying and mixing pipeline connected with a wax oil inlet, an automatic regulating valve is arranged on the pipeline, the other branch pipeline is a heat exchange wax oil pipeline connected with a heat exchange spray head, and the pipeline is provided with the automatic regulating valve; the circulating oil outlet is connected with a circulating oil pipeline through a filter, an automatic regulating valve is arranged on the pipeline, a branch pipeline is arranged at the downstream of the filter and is a washing circulating oil pipeline, the washing circulating oil pipeline is connected with a washing spray head, the automatic regulating valve and a flowmeter are arranged on the pipeline, an oil gas outlet and an oil gas outlet pipeline are connected to a fractionating tower, a thermometer is arranged on the pipeline, and a liquid level meter is arranged at the lower part of the tank body.
The oil gas at the top of the coke tower and the oil gas spraying wax mixing oil respectively enter an oil gas heat exchange washing tank 12 from an oil gas inlet 1 and a wax oil inlet 2, so that the oil gas at the top of the coke tower and the oil gas spraying wax mixing oil are fully mixed in an inner cylinder 6 to obtain mixed oil gas. Oil gas spraying mixed wax oil in the oil gas spray pipe 3 is divided into cooling wax oil of the fractionating tower, the feeding flow of the oil gas spraying mixed wax oil is adjusted by a flowmeter 14-1 through an automatic adjusting valve 17-1 according to the flow of tower top oil gas, and the cooling wax oil of the fractionating tower is divided into wax oil distilled from the fractionating tower; the mixed oil gas and the atomized oil gas heat exchange wax oil sprayed by the heat exchange spray head 7 are contacted for heat exchange. Oil gas heat exchange wax oil is divided into cooling wax oil of a fractionating tower, and the oil gas heat exchange wax oil feeding flow is adjusted by a thermometer 16 through an automatic adjusting valve 17-2 according to the temperature of oil gas subjected to heat exchange washing and sent to the fractionating tower; the mixed oil gas after heat exchange is washed by the atomized washing circulating oil sprayed by the washing nozzle 8. The washing circulating oil is divided into circulating oil after being decoked by the filter 13, and the feeding flow of the washing circulating oil is adjusted by the flowmeter 14-2 through the automatic adjusting valve 17-3 according to the flow per se; the washed mixed oil gas is subjected to gas-liquid two-phase high-efficiency cyclone separation through a cyclone plate 9; after the oil gas after gas-liquid separation is settled by gravity, the oil gas flows to a fractionating tower through an oil gas outlet 5 at the conical section of a tank body 10, the circulating oil containing coke powder is settled to the bottom of the tank body 10, the coke powder is removed from a circulating oil outlet 11 through a filter 13, one part of the circulating oil flows to a washing spray head 8, and the other part of the circulating oil flows to the fractionating tower. The flow rate of the circulating oil is adjusted by a liquid level meter 15 according to the liquid level in the tank through an automatic adjusting valve 17-4.
Examples
The invention is further illustrated below with reference to specific examples. It is to be understood, however, that these examples are illustrative only and are not to be construed as limiting the scope of the present invention. Test methods in which specific conditions are not specified in the following examples are generally carried out under conventional conditions or under conditions recommended by the manufacturer. All percentages and parts are by weight unless otherwise indicated.
The delayed coking device of Shanghai chemical plant adopts a device and a method for oil gas heat exchange washing as shown in figure 1 to carry out the process treatments of mixing, cooling heat exchange, washing and coke deposition, gas-liquid separation and the like on the oil gas at the tower top, and most of coke powder in the oil gas at the tower top is washed into the circulating oil, thereby reducing the coke powder content entering a fractionating tower, wherein
(1) Process conditions
The mass concentration of coke powder in oil gas at the top of the coking tower is 87mg/L, and the temperature of the oil gas at the top of the coking tower is 420 ℃.
(2) Process flow and apparatus
As illustrated in fig. 1 and the detailed description.
(3) Application effects
By using the device and the method, the coke powder mass concentration at the oil gas inlet of the fractionating tower is reduced to be below 5mg/L, the coke powder removal rate reaches more than 94 percent, the coke powder amount entering the fractionating tower along with the oil gas is effectively reduced, the product quality of the delayed coking device is further improved, the running period of the delayed coking device and downstream devices is prolonged, and the operation cost is saved.
Claims (8)
1. An apparatus for heat-exchanging scrubbing of oil and gas, the apparatus comprising:
the oil-gas heat exchange washing tank comprises an oil-gas inlet, a wax oil spray pipe, an oil-gas outlet, an inner cylinder, a heat exchange spray head, a washing spray head, a rotational flow plate, a tank body and a circulating oil outlet;
the oil-gas heat exchange washing tank is arranged behind the coking tower, the upper part of the oil-gas heat exchange washing tank is provided with a wax oil spray pipe wrapping an oil-gas spray pipe, an oil-gas inlet is arranged at the top of the oil-gas spray pipe and is positioned at the upper part of a column section of the wax oil spray pipe, an outlet at the lower part of the wax oil spray pipe is connected with an inner cylinder, so that oil gas at the top of the coke tower and oil gas sprayed and mixed wax oil are fully mixed in the inner cylinder to obtain mixed oil gas, a hot spray head and a washing spray head are arranged in the inner cylinder from top to bottom, the spraying directions of the heat exchange spray head and the washing spray head are opposite to the flowing direction of the mixed oil gas, a rotational flow plate is arranged at the bottom of the inner cylinder, the tank body is a vertical pressure container, a circulating oil outlet is arranged at the bottom of the tank body, and the oil gas outlet is arranged at a conical section of the tank body;
the tower top oil gas pipeline is connected with an oil gas inlet, and a flowmeter is arranged on the pipeline; the cooling wax oil pipeline from the fractionating tower is provided with two branch pipelines, one branch pipeline is a wax oil spraying and mixing pipeline connected with a wax oil inlet, an automatic regulating valve is arranged on the pipeline, the other branch pipeline is a heat exchange wax oil pipeline connected with a heat exchange spray head, and the pipeline is provided with the automatic regulating valve; the circulating oil outlet is connected with a circulating oil pipeline through a filter, an automatic regulating valve is arranged on the pipeline, a branch pipeline is arranged at the downstream of the filter and is a washing circulating oil pipeline, the washing circulating oil pipeline is connected with a washing spray head, the automatic regulating valve and a flowmeter are arranged on the pipeline, an oil gas outlet and an oil gas outlet pipeline are connected to a fractionating tower, a thermometer is arranged on the pipeline, and a liquid level meter is arranged at the lower part of the tank body;
the upper part of the wax oil spray pipe is conical, and the included angle between the conical surface and the central axis is 37-52 degrees; the lower parts of the oil gas spray pipe and the wax oil spray pipe are designed to be conical, and the included angle between the conical surface and the central axis is 24-37 degrees;
the heat exchange spray head and the washing spray head are nozzle type distributors, the distance between the heat exchange spray head and the outlet of the spray pipe is 0.1-0.18 of the length of the tank body, and the distance between the washing spray head and the heat exchange spray head is 0.07-0.12 of the length of the tank body.
2. The apparatus as claimed in claim 1, wherein the cyclone plate is connected to the bottom of the inner tub at a distance of 0.12-0.2 the length of the can body from the washing nozzle, and the cyclone plate has a thickness of 0.02-0.05 the length of the can body.
3. The apparatus of claim 1, wherein the ratio of the diameter of said can to said inner barrel is in the range of 1.2 to 1.5.
4. A method of oil and gas heat exchange scrubbing of the apparatus of claim 1, comprising the steps of:
(a) the method comprises the following steps that oil gas and oil gas sprayed and mixed wax oil on the top of a coke tower enter an oil gas heat exchange washing tank from an oil gas inlet and a wax oil inlet respectively, so that the oil gas on the top of the coke tower and the oil gas sprayed and mixed wax oil are fully mixed in an inner cylinder to obtain mixed oil gas, the oil gas sprayed and mixed wax oil in an oil gas spraying pipe is used for shunting cooling wax oil of a fractionating tower, the feeding flow of the oil gas sprayed and mixed wax oil is adjusted by a flowmeter through an automatic adjusting valve according to the flow of the oil gas on the top of the coke tower, and the cooling wax oil of the fractionating tower is used for shunting the wax oil distilled from the fractionating tower;
(b) contacting the mixed oil gas obtained in the step (a) with atomized oil gas heat exchange wax oil sprayed by a heat exchange spray head for heat exchange, wherein the oil gas heat exchange wax oil is used for shunting cooling wax oil of a fractionating tower, and the feeding flow of the oil gas heat exchange wax oil is adjusted by a thermometer through an automatic adjusting valve according to the temperature of the oil gas subjected to heat exchange washing in the fractionating tower;
(c) flushing and washing the mixed oil gas subjected to heat exchange in the step (b) and atomized washing circulating oil sprayed by a washing spray head, wherein the washing circulating oil is divided into circulating oil subjected to filter decoking, and the feeding flow of the washing circulating oil is adjusted by a flowmeter through an automatic adjusting valve according to the flow per se;
(d) carrying out gas-liquid two-phase cyclone separation on the mixed oil gas washed in the step (c) through a cyclone plate;
(e) and (d) allowing oil gas subjected to gas-liquid separation in the step (d) to flow to a fractionating tower through an oil gas outlet of a tank body conical section after gravity settling, allowing circulating oil containing coke powder to settle to the bottom of the tank body, removing the coke powder from the circulating oil outlet through a filter, allowing one part of the circulating oil to flow to a washing spray head and the other part of the circulating oil to flow to the fractionating tower, and adjusting the flow of the circulating oil through an automatic regulating valve by a liquid level meter according to the liquid level in the tank.
5. The method as claimed in claim 4, wherein in step (a), the temperature of the oil gas at the top of the oil gas inlet is 380-420 ℃, and the flow ratio of the oil gas at the top of the tower to the oil gas mixed wax oil is 0.3-0.7.
6. The method of claim 4, wherein in step (b), the heat exchange nozzle atomizes liquid droplets having a diameter of 0.5-1mm, an average particle diameter of 0.7-0.8mm, and the heat exchange circulating oil has a flow rate of 0.8-1.2 of the oil gas flow rate.
7. The method of claim 4, wherein in step (c), the diameter of the liquid droplets atomized by the washing nozzle is 0.6 to 1.2mm, the average particle diameter is 0.8 to 0.9mm, and the flow rate of the washing circulation oil is 1.3 to 1.8 of the oil gas flow rate.
8. The method of claim 4, wherein in step (e), the level of the wax oil in the oil-gas heat exchange washing tank is not higher than 90% of the height from the bottom of the tank body to the bottom of the cyclone plate, and the temperature of the oil gas flowing out of the conical section of the tank body after heat exchange washing is 370-400 ℃.
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