CN112500882B - Method for adjusting catalytic cracking main fractionating tower to increase yield of aviation kerosene fraction - Google Patents
Method for adjusting catalytic cracking main fractionating tower to increase yield of aviation kerosene fraction Download PDFInfo
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- CN112500882B CN112500882B CN202011369045.8A CN202011369045A CN112500882B CN 112500882 B CN112500882 B CN 112500882B CN 202011369045 A CN202011369045 A CN 202011369045A CN 112500882 B CN112500882 B CN 112500882B
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- 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
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Abstract
The invention relates to a method for increasing yield of aviation kerosene fraction by reforming a catalytic cracking main fractionating tower. The method comprises the following steps: s1, dismantling a plurality of tower plates from the upper part of the light diesel oil extraction hopper to the lower part of the top circulating extraction hopper, and arranging a filler A and an oil collecting tank A from top to bottom; wherein the oil collecting tank A can draw out the aviation coal fraction to be sent to an aviation coal refining device; s2, dismantling a plurality of tower plates below the rich absorption oil inlet, and arranging a liquid distributor B, a filler B and a fuel collection tank B from top to bottom; wherein the oil collecting tank B can draw out light diesel oil fraction; and S3, the aviation kerosene fraction stripping tower utilizes the original heavy diesel oil stripping tower, the aviation kerosene fraction enters the aviation kerosene fraction stripping tower for stripping, the aviation kerosene fraction is cooled and sent to an aviation kerosene refining device, and the extraction amount of the aviation kerosene fraction controls the 95% distillation point of the aviation kerosene fraction. The method increases the aviation kerosene extraction line of the qualified aviation kerosene distillation range of the catalytic unit fractionation system by measures such as reforming partial tower trays of the catalytic cracking unit fractionation tower, fully utilizes the existing conditions of the original unit, reduces the modification engineering amount, saves the investment and has important guiding significance for increasing the aviation kerosene production of the refinery.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a method for adjusting a catalytic cracking main fractionating tower to increase the yield of aviation kerosene fraction.
Background
The demand of China civil aviation industry for aviation kerosene (referred to as aviation kerosene, the same is used hereinafter) is increased rigidly, and the increase of production of aviation kerosene is the transformation and upgrading direction of fuel type oil refining enterprises. Part of catalytic diesel oil which accords with the distillation range of the aviation kerosene is added into a aviation kerosene hydrofining device to be processed into qualified aviation kerosene, so that the catalytic diesel oil has better feasibility and considerable investment income and is gradually valued by petrochemical enterprises. The distillation range of the aviation kerosene generally requires that the temperature of 95 percent of the distillation point is less than or equal to 260 ℃ and the temperature of 95 percent of the distillation point of the diesel oil is less than or equal to 365 ℃, and in view of the different distillation ranges of the catalytic diesel oil and the aviation kerosene, if the diesel oil is directly introduced into the aviation kerosene hydrofining to influence the distillation range of the aviation kerosene, the coking of the catalyst of the aviation kerosene hydrofining device is also accelerated, and the load and the consumption of the aviation kerosene hydrofining device are increased. Therefore, under the condition of not influencing the distillation process of the existing diesel oil fraction, how to simply, rapidly and efficiently obtain the aviation kerosene extraction line which accords with the distillation process of aviation kerosene from the new increase and separation of the existing catalytic device distillation system is a worth of discussion.
The catalytic cracking fractionating tower belongs to a rectifying tower, but only has a feeding section and a rectifying section, a reaction oil-gas mixture is gradually partially cooled by each reflux, and oil slurry, recycle oil, light diesel oil and tower top oil gas (containing gasoline, rich gas and steam components) are gradually obtained from bottom to top, wherein the temperature of 95 percent of the distillation point of the light diesel oil is less than or equal to 365 ℃, the blending requirement of the diesel oil for vehicles is met, and the existing process is provided with a non-aviation kerosene fraction extraction section.
The inner components of the fractionating tower mainly comprise tower plates and fillers, and the plate-type tower becomes the main equipment of the separation engineering in the past decades due to the characteristics of stable operation, higher mass transfer efficiency, simple installation and the like. Compared with a plate tower, the grid packing in the regular packing is high-clearance packing, and is particularly suitable for occasions with large load, small pressure drop, heavier media and solid particles; the plate corrugated structured packing is suitable for low-pressure-drop fractionation occasions with high fractionation requirements. The design of the liquid distributor of the packed tower is also critical to the tower load, and the operation elasticity of the packed tower can be determined according to actual requirements, so that the tower has higher operation elasticity. In the development of the trays and packing respectively, it is also conceivable to combine the advantages of both into a combined column internal. Attempts to replace some or all of the trays of the established tray column with packing have also been reported. The tower plates of different tower sections of a 50kt/a catalytic cracking fractionating tower are replaced by pore plate corrugated packing with different specifications in 1992 by adopting the modified design [ J ] of regular packing, oil refining design, 1992(22): 59-63) and the like of a mature maple (mature maple, xianxiao, and the like) of Daqing petrochemical institute, so that the treatment capacity of the device reaches 3 times of the original capacity. In the case of the conventional 2.0Mt/t catalytic cracking fractionating tower, 1-17 layers and a desuperheating section are replaced by 5 sections of packing under the condition that the tower height and the tower diameter are not changed, and the rest tower plates are replaced by Grignard efficient tower plates, so that the processing capacity is improved to 2.8 Mt/a. Transformation of a main fractionating tower of a catalytic cracking device in a Luoyang petrochemical industry (Zhang Feng, Houyubao, and the like) [ J ],2009(39)9: 13-15), partial double overflow tower plates of the main fractionating tower are changed into four overflow tower plates before and after 2008, a tongue fixing tower plate is changed into a high-performance MVG fixed valve tower plate, and a herringbone tower plate at the bottom of the tower is changed into regular grid packing; after the device is transformed, the processing capacity of the device is improved, the operation elasticity is increased, and the tower pressure drop is reduced. The modification of the interior of the existing catalytic cracking main fractionating tower has no report of changing or increasing the extract line fraction of the main fractionating tower (the composition of each extract line is determined by the distillation range), and no report of extracting the aviation kerosene fraction which accords with the aviation kerosene distillation range by modifying tower internals and the like.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provides a method for adjusting a catalytic cracking main fractionating tower to increase the yield of aviation kerosene fractions. The method for adjusting the catalytic cracking main fractionating tower to increase the yield of the aviation kerosene fraction is characterized in that tower internals of partial fractionating sections of the existing catalytic cracking fractionating tower are modified or replaced, a aviation kerosene extraction line of a qualified aviation kerosene distillation range is added to a catalytic device fractionating system, and a diesel oil stripping tower is modified to improve the fractionating efficiency.
The invention can solve the problems by the following technical scheme: a method for adjusting a catalytic cracking main fractionating tower to increase the yield of aviation kerosene fraction comprises the following steps:
the process for improving the fractionation efficiency by reforming part of the fractionation sections of the existing catalytic cracking fractionating tower and reforming the diesel oil stripping tower comprises the following steps:
s1, dismantling a plurality of tower plates above an rich absorption oil inlet of a catalytic cracking main fractionating tower, and arranging a liquid collecting distributor A, a filler A and an oil collecting tank A in the tower from top to bottom at the position of the dismantled tower plates; wherein the oil collecting tank A can draw out the aviation kerosene fraction to enter an aviation kerosene stripping tower;
s2, dismantling a plurality of tower plates below an rich absorption oil inlet of the catalytic cracking main fractionating tower, and arranging a liquid collecting distributor B, a filler B and a fuel collecting tank B in the tower from top to bottom at the position of the dismantled tower plates; wherein the oil collecting tank B can draw out light diesel oil fraction;
s3, step S1 aviation kerosene fraction stripping tower utilizes the original heavy diesel oil stripping tower, and corrugated packing is adopted in the tower; the aviation kerosene fraction enters an aviation kerosene fraction stripping tower for stripping; a flow control valve group of a aviation kerosene fraction outlet device is added, and the 95% distillation point of the aviation kerosene fraction outlet device is controlled by utilizing the extraction amount of the aviation kerosene fraction;
s4, the step S2 the light diesel oil fraction enters a light diesel oil stripping tower for stripping; the 95 percent of the distillation point of the light diesel oil is controlled by controlling the extraction amount of the light diesel oil.
The proportion range of the demolition tower plate above the rich absorption oil inlet in the S1 in the whole tower plate is 18-23%; the proportion of the demolition tower plate below the rich absorption oil inlet in the S2 accounts for 8-13% of the whole tower plate.
The original rich absorption oil inlet of the catalytic cracking main fractionating tower is reserved, and the liquid phase part in the rich absorption oil and part of liquid flowing down from the oil collecting tank A enter the liquid collecting distributor B together.
The filler A is regular corrugated filler; the filler B is regular grid filler; the regular corrugated packing is one of silk screen corrugated packing and plate corrugated packing; the regular grid packing is one of Grignard grid packing and mesh grid packing.
And the liquid collecting distributor A and the liquid collecting distributor B respectively adopt a trough-tray type liquid distributor.
The proportion range of the height of the filler A in the height of the whole tower plate is 18-23%; the proportion range of the height of the filler B in the height of the whole tower plate is 8-13%.
The space between the filler A and the liquid collecting distributor A and the space between the filler B and the liquid collecting distributor B account for 5-7% of the height of the tower plate of the whole tower.
Compared with the background technology, the invention has the following beneficial effects: the invention relates to a aviation kerosene extraction line which increases a qualified aviation kerosene distillation range of a catalytic device fractionation system by measures such as reforming part of tower internals of a catalytic cracking device fractionation tower. The invention fully utilizes the existing conditions of the original device, partially reforms the catalytic cracking fractionating tower and related devices on the premise of meeting the process requirements and standard specifications, and extracts the aviation kerosene fraction meeting the aviation kerosene distillation range on the premise of not influencing the diesel oil distillation range.
The method of the invention can utilize the existing equipment as much as possible, reduce the amount of changed engineering and save the investment. The invention has important guiding significance for increasing the yield of aviation kerosene of the existing refining enterprises.
When the regular packing is selected, the packing properties such as specific surfaces, void ratios and the like of different regular packings are fully considered, and the regular corrugated packing with small void ratio is selected as the liquid flow in the upper packing section of the invention is relatively small; and the lower packing section returns a large amount of rich absorption oil to the main fractionating tower, so that the liquid flow is increased rapidly, and regular grid packing with high void ratio is selected.
Drawings
FIG. 1 is a schematic diagram of a reforming section and a stripping column of a catalytic cracking main fractionator according to the present invention.
In the figure: 1-upper tower plate of a filler section, 2-liquid collecting distributor A, 3-filler A, 4-oil collecting tank A, 5-aviation kerosene fraction extraction line, 6-liquid collecting distributor B, 7-filler B, 8-light diesel oil fraction extraction line, 9-oil collecting tank B, 10-rich absorption oil inlet, 11-lower tower plate of the filler section, 12-aviation kerosene fraction stripping tower and 13-light diesel oil fraction stripping tower.
The specific implementation mode is as follows:
the invention will be further described with reference to the following drawings and specific embodiments:
a method for adjusting catalytic cracking main fractionating tower to increase production of aviation kerosene fraction, wherein 3-6 tower plates above a rich absorption oil inlet 10 of the catalytic cracking main fractionating tower are dismantled, and the fraction oil meets requirements of aviation kerosene fraction and meets 95% of fraction point temperature of less than or equal to 260 ℃ according to fraction distribution calculation of the fractionating tower, so that the fraction can be extracted at the position; a liquid collecting distributor A2, a filler A3 and an oil collecting tank A4 are arranged in the tower; wherein the oil collecting tank A4 can extract the aviation kerosene fraction by adding an aviation kerosene fraction extraction line 5, and the aviation kerosene fraction is extracted and enters an aviation kerosene fraction stripping tower 12 for stripping; a flow control valve group of a aviation kerosene fraction outlet device is added, and the 95% distillation point of the aviation kerosene fraction outlet device is controlled by utilizing the extraction amount of the aviation kerosene fraction; removing 4-7 tower plates below the rich absorption oil inlet, and arranging a liquid collecting distributor B6, a filler B7 and a fuel collecting tank B9 in the tower; the float valve tray is removed and replaced by high-efficiency filler, and the temperature of 95 percent of the distillation point of the light diesel oil fraction is ensured to be less than or equal to 365 ℃ under the condition that the diameter of the tower is unchanged and the number of effective plates is reduced; wherein the oil collecting tank B9 can extract light diesel oil fraction by adding a light diesel oil fraction extraction line 8, and the extracted light diesel oil fraction enters a light diesel oil fraction stripping tower 13 for stripping; controlling the 95 percent of distillation point of the light diesel oil by controlling the extraction amount of the light diesel oil; the top of the filler A3 is a filler section upper tower plate 1; the bottom of the filler B7 is a lower tray 11 of the filler section; the liquid collecting distributor A2 and the liquid collecting distributor B6 are trough-tray type liquid collecting distributors respectively.
The proportion range of the height of the filler A in the height of the whole tower plate is 20 percent; the proportion range of the height of the filler B in the height of the whole tower plate is 10 percent; by adopting the proportion, under the condition that the tower diameter is not changed, the aviation kerosene fraction extraction section is added, the effective plate number is reduced, and in order to ensure that 95 percent of the distillation point temperature of the aviation kerosene fraction and the light diesel oil fraction is qualified, efficient packing with better efficiency is adopted.
The aviation kerosene fraction stripping tower is an old original heavy diesel oil stripping tower, and corrugated packing is adopted in the tower; the aviation kerosene fraction enters a pipeline at the upper part of an aviation kerosene fraction stripping tower, is in reverse contact with steam entering at the bottom, and is extracted from the top of the tower to obtain non-condensable gas after stripping, and is extracted from the bottom of the tower to obtain aviation kerosene fraction after stripping; and a flow control valve group of a aviation kerosene fraction outlet device is added, and the 95% distillation point of the aviation kerosene fraction outlet device is controlled by utilizing the extraction amount of the aviation kerosene fraction.
The light diesel oil fraction enters an upper pipeline of a light diesel oil stripping tower and is in reverse contact with steam entering from the bottom, the non-condensable gas stripped from the top of the tower is extracted, and the light diesel oil fraction stripped from the bottom of the tower is extracted; the 95 percent of the distillation point of the light diesel oil is controlled by controlling the extraction amount of the light diesel oil.
The original rich absorption oil inlet is reserved, and the liquid phase part in the rich absorption oil enters the liquid collecting distributor B together with the part of liquid which is shunted by the oil collecting tank A.
The filler A is regular corrugated filler; the corrugated packing can be one of wire mesh corrugated packing and plate corrugated packing; the filler B is regular grid filler; the grid filler is one of Grignard grid filler and mesh grid filler.
When the liquid flows downwards along the packing layer, the liquid flows towards the wall of the tower, and the phenomenon is called wall flow and wall flow, which causes uneven gas-liquid distribution in the packing layer, so that the mass transfer efficiency is reduced. In order to reduce the influence of the wall flow phenomenon, a liquid collecting and redistributing device can be arranged below the packing layer at certain intervals; the space between the filler A and the liquid collecting distributor A and the space between the filler B and the liquid collecting distributor B account for 5 percent of the height of the tower plate of the whole tower; the proportion can also meet the requirements of sufficient oil collecting tank volume and uniform liquid distribution.
The liquid collecting distributor A has the functions of collecting oil and separating liquid, collects the liquid from the upper tower plate and redistributes the collected liquid so as to uniformly enter the filler at the lower part; the liquid collecting distributor A adopts a trough-tray type liquid collecting distributor.
The oil collecting tank A is a liquid collecting device and has larger liquid collecting amount. Collecting liquid flowing down from the section A of the filler, and taking part of the liquid as aviation kerosene fraction through a pumping outlet to enter an aviation kerosene fraction stripping tower; the other liquid passes over the weir of the oil collector in the oil collecting tank A and enters the liquid collecting distributor B below.
The liquid collecting distributor B simultaneously receives partial liquid which is shunted by the oil collector in the oil collecting tank A and the rich absorption oil which returns to the fractionating tower, and simultaneously redistributes the collected liquid to ensure that the collected liquid uniformly enters the filler at the lower part; the liquid collecting distributor B adopts a trough-tray type liquid collecting distributor.
The liquid collecting device of the oil collecting tank B has larger liquid collecting amount. Collecting liquid flowing down from the section B of the filler, and taking part of the liquid as diesel oil fraction through a suction port; the other part of the liquid passes over the plate weir of the oil collector 2 in the oil collecting tank B and enters the liquid collecting tank of the lower tower plate.
When the regular packing is selected, the packing properties such as specific surfaces, void ratios and the like of different regular packings are fully considered, and the regular corrugated packing with small void ratio is selected as the liquid flow in the upper packing section of the invention is relatively small; and the lower packing section returns a large amount of rich absorption oil to the main fractionating tower, so that the liquid flow is increased rapidly, and regular grid packing with high void ratio is selected.
Example 1
The processing capacity of a main fractionating tower of a catalytic cracking device of a certain refinery is 150t/h, the main fractionating tower has 32 tower plates, the tower plates are sequentially 1-32 tower plates from bottom to top, the tower plates 24-27 at the upper part and 19-23 at the lower part of an rich absorption oil inlet of the main fractionating tower are respectively dismantled, and 250Y pore plate corrugated packing and Grignard packing are respectively replaced in the tower at the positions of the tower plates dismantled at the upper part and the lower part of the rich absorption oil inlet; the heights of the two sections of the 250Y pore plate corrugated packing and the Grignard packing are respectively 1.3 m and 1.5 m, and a groove type liquid collecting distributor and an oil collector with large oil storage capacity are respectively arranged at the top and the bottom of the 250Y pore plate corrugated packing and the Grignard packing at the interval of 2.35 m.
The oil collector at the bottom of the upper section of the filler can extract 5-8 t/h of aviation kerosene distillate oil, the aviation kerosene distillate oil enters the modified aviation kerosene distillate stripping tower, and the aviation kerosene distillate oil is subjected to heat exchange to reach a qualified temperature and then can be mixed into the raw material of the aviation kerosene hydrogenation modification device. Sampling and detecting that the 95 percent of the distillation point temperature of the stripped aviation kerosene fraction is 252-259 ℃. Through the technical improvement, the refinery can increase the yield of the aviation kerosene by 4-6.4 ten thousand tons every year.
The present invention provides a method for reforming a catalytic cracker main fractionator, which has been described by way of example, it will be apparent to those skilled in the art that the technique of the present invention can be implemented by modifying or appropriately changing and combining the contents described herein without departing from the contents, spirit and scope of the present invention. It is expressly intended that all such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the spirit, scope and content of the invention.
Claims (5)
1. A method for adjusting a catalytic cracking main fractionating tower to increase the yield of aviation kerosene fraction is provided, a part of fractionating sections of the existing catalytic cracking fractionating tower are modified, and a diesel oil stripping tower is modified to improve the process of the fractionating efficiency, and the method comprises the following steps:
s1, dismantling a plurality of tower plates above an rich absorption oil inlet of a catalytic cracking main fractionating tower, and arranging a liquid collecting distributor A, a filler A and an oil collecting tank A in the tower from top to bottom at the position of the dismantled tower plates; wherein the oil collecting tank A can draw out the aviation kerosene fraction to enter an aviation kerosene stripping tower;
s2, dismantling a plurality of tower plates below an rich absorption oil inlet of the catalytic cracking main fractionating tower, and arranging a liquid collecting distributor B, a filler B and a fuel collecting tank B in the tower from top to bottom at the position of the dismantled tower plates; wherein the oil collecting tank B can draw out light diesel oil fraction;
s3, the aviation kerosene fraction stripping tower of the step S1 utilizes the original heavy diesel oil stripping tower, and the aviation kerosene fraction enters the aviation kerosene fraction stripping tower to be stripped; a flow control valve group of a aviation kerosene fraction outlet device is added, and the 95% distillation point of the aviation kerosene fraction outlet device is controlled by utilizing the extraction amount of the aviation kerosene fraction;
s4, the step S2 the light diesel oil fraction enters a light diesel oil stripping tower for stripping; controlling the 95 percent of distillation point of the light diesel oil by controlling the extraction amount of the light diesel oil;
the proportion range of the demolition tower plate above the rich absorption oil inlet in the S1 in the whole tower plate is 18-23%;
the proportion of the demolition tower plate below the rich absorption oil inlet in the S2 accounts for 8-13% of the whole tower plate;
the proportion range of the height of the filler A in the height of the whole tower plate is 18-23%; the proportion range of the height of the filler B in the height of the whole tower plate is 8-13%;
the space between the filler A and the liquid collecting distributor A and the space between the filler B and the liquid collecting distributor B account for 5-7% of the height of the tower plate of the whole tower.
2. The method for adjusting the catalytic cracking main fractionator for stimulation of aviation kerosene distillate according to claim 1, wherein: the original rich absorption oil inlet of the catalytic cracking main fractionating tower is reserved, and the liquid phase part in the rich absorption oil and part of liquid flowing down from the oil collecting tank A enter the liquid collecting distributor B together.
3. The method for adjusting the catalytic cracking main fractionator for stimulation of aviation kerosene distillate according to claim 1, wherein: the filler A is regular corrugated filler; the packing B is a regular grid packing.
4. The method for adjusting the catalytic cracking main fractionator for stimulation of aviation kerosene distillate according to claim 3, wherein: the regular corrugated packing is one of silk screen corrugated packing and plate corrugated packing; the regular grid packing is one of Grignard grid packing and mesh grid packing.
5. The method for adjusting the catalytic cracking main fractionator for stimulation of aviation kerosene distillate according to claim 1, wherein: and the liquid collecting distributor A and the liquid collecting distributor B respectively adopt a trough-tray type liquid distributor.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203419880U (en) * | 2013-08-29 | 2014-02-05 | 刘英聚 | Light gasoline, heavy gasoline and light diesel oil separation device |
| CN203569037U (en) * | 2013-11-12 | 2014-04-30 | 中石化洛阳工程有限公司 | Fractionating tower |
| CN106433771A (en) * | 2016-10-26 | 2017-02-22 | 华南理工大学 | Low-energy-consumption catalytic cracking and catalytic gasoline selective hydrogenation combined process |
| CN110354518A (en) * | 2019-08-12 | 2019-10-22 | 无锡科技职业学院 | A kind of atmospheric and vacuum tower |
-
2020
- 2020-11-30 CN CN202011369045.8A patent/CN112500882B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203419880U (en) * | 2013-08-29 | 2014-02-05 | 刘英聚 | Light gasoline, heavy gasoline and light diesel oil separation device |
| CN203569037U (en) * | 2013-11-12 | 2014-04-30 | 中石化洛阳工程有限公司 | Fractionating tower |
| CN106433771A (en) * | 2016-10-26 | 2017-02-22 | 华南理工大学 | Low-energy-consumption catalytic cracking and catalytic gasoline selective hydrogenation combined process |
| CN110354518A (en) * | 2019-08-12 | 2019-10-22 | 无锡科技职业学院 | A kind of atmospheric and vacuum tower |
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