CN213623996U

CN213623996U - Processing system for condensed oil in preheating oil throwing stage of coke tower of delayed coking device

Info

Publication number: CN213623996U
Application number: CN202022857882.7U
Authority: CN
Inventors: 王义鹏; 田茂良; 彭昌会; 王骄; 刘哲
Original assignee: Shandong Huifeng Petrochemical Group Co ltd
Current assignee: Shandong Huifeng Petrochemical Group Co ltd
Priority date: 2020-12-01
Filing date: 2020-12-01
Publication date: 2021-07-06
Anticipated expiration: 2030-12-01

Abstract

The utility model belongs to the technical field of the delayed coking device, concretely relates to delayed coking device coke tower preheats processing system who gets rid of oil stage condensate oil, including getting rid of oil tank and fractionating tower, the fractionating tower is connected with reaction oil gas line, is equipped with the wax oil sump oil case in the fractionating tower, and the wax oil sump oil case is connected with wax oil extraction pipe, and wax oil extraction pipe is connected with the fractionating tower on wax oil sump oil case upper portion through wax oil upper portion return line, gets rid of the oil tank and is connected with the vent tower through the atmospheric valve, gets rid of the oil tank and is connected with wax oil upper portion return line through the wax oil valve. When the coke tower is preheated to throw off oil, the condensed oil does not directly enter the bottom of the fractionating tower, so that the increase of the running circulation ratio of the device is avoided, the treatment capacity of fresh feeding is ensured, and the amount of the wax oil refined back can be reduced by 20-30t in each production period; meanwhile, the wax oil collecting tank is improved by throwing the wax oil, so that the yield of the wax oil of the device is increased, and the delivery amount of the wax oil is increased by 30-40t in each production period. Not only can reduce the circulation ratio, but also can increase the yield of wax oil.

Description

Processing system for condensed oil in preheating oil throwing stage of coke tower of delayed coking device

Technical Field

The utility model belongs to the technical field of delay coking device, concretely relates to processing system of oil stage condensate oil is got rid of in preheating of delay coking device coke drum.

Background

At present, delayed coking devices of petrochemical enterprises in China mostly operate intermittently by two coke drums, wherein the generation of oil throwing (warm drum condensed oil) is determined by the particularity of semi-continuous operation of the coke drums. Because the empty coke tower after coke removal is in a normal temperature state, the temperature difference between the empty coke tower and the feeding temperature (480 ℃) for switching green coke is large, the problem of expansion with heat and contraction with cold of the coke tower is considered, and in order to prolong the service life of the coke tower, the empty coke tower of the coke tower needs to be preheated before being switched to the green coke tower. The heat source for preheating comes from high-temperature oil gas (about 420 ℃) at the top of the green coke tower. Condensed oil is inevitably formed after the high-temperature oil gas enters the empty tower, and the condensed oil mainly comprises diesel oil and wax oil, but also contains a small amount of condensed water which needs to be removed. Most of the existing methods for removing condensed water are methods of removing condensed water in an emptying tower in the early stage of oil throwing (before the bottom temperature of coke tower is 180 ℃), and changing the method into a method of removing condensed water in the bottom of a fractionating tower in the later stage. But because the temperature of the oil throwing is low, the oil is mixed with the raw materials when entering the bottom of the fractionating tower, so that the operation circulation ratio of the device is increased, the processing capacity of the raw materials is reduced, and the energy consumption and the operation cost of the device are increased; in addition, the temperature of oil gas can be reduced when the condensed oil enters the tower bottom, so that the heat balance in the original fractionating tower is broken, the overall temperature of the fractionating tower is reduced, and the product quality is easily influenced.

The recycle ratio for a coker fractionator is (radiant dose-to-flow)/to-flow. The convection flow refers to the feeding flow of the coking raw material at the lower part of the fractionating tower after being heated by the convection chamber of the heating furnace, and the radiant quantity refers to the flow of the bottom oil of the fractionating tower which is pumped out by a pump, heated by the radiant chamber of the heating furnace and then enters the coke tower. The bottom oil of the fractionating tower is mostly from convection feeding, a part of heavy components in oil gas from the top of the coke tower are condensed at the lower part of the fractionating tower and reflows to heavy oil at the lower part of the fractionating tower, the part of oil enters the coke tower as a gas phase and is condensed in the fractionating tower to be pumped out by a radiation pump, and the circulating oil is the circulating oil. Therefore, the radiation quantity minus the quantity of the circulating oil at the flow rate can be roughly divided by the feed flow rate, namely the flow rate is the circulation ratio. Briefly, convection can be understood as the amount of fresh oil and radiation can be understood as the amount of cycle oil and fresh residual oil!

The formula is as follows: the recycle ratio (radiant dose-fresh feed dose)/fresh feed dose.

The large circulation ratio can produce more gasoline and diesel oil, but the coke production amount and the dry gas amount are also greatly increased, the energy consumption of the device is increased, and the processing capacity of the device is reduced. The adoption of a small circulation ratio can integrally improve the yield of the device, reduce energy consumption and increase the processing capacity of the device. The reduction of the circulation ratio is one of the development trends of the delayed coking process, and the aim is to increase the yield of catalytic cracking and hydrocracking raw oil by increasing the yield of coking wax oil.

SUMMERY OF THE UTILITY MODEL

The to-be-solved technical problem of the utility model is: the defects of the prior art are overcome, the processing system for the condensed oil in the preheating and oil throwing stage of the coke tower of the delayed coking device is provided, when the coke tower preheats and throws the oil, the condensed oil does not directly enter the bottom of the fractionating tower, the increase of the running circulation ratio of the device is avoided, the processing amount of fresh feeding is ensured, and meanwhile, the yield of the wax oil can be increased.

The utility model discloses an adopt following technical scheme to realize:

the processing system of the condensed oil in the preheating and oil throwing stage of the coke tower of the delayed coking device comprises an oil throwing tank and a fractionating tower, wherein the fractionating tower is connected with a reaction oil gas line from the delayed coking coke tower, a wax oil collecting tank is arranged in the fractionating tower and is connected with a wax oil extracting pipe, the wax oil extracting pipe is connected with the fractionating tower on the upper part of the wax oil collecting tank through a wax oil upper part return line, the oil throwing tank is connected with an emptying tower through an emptying valve, and the oil throwing tank is connected with the wax oil upper part return line through a wax oil valve.

Preferably, an oil throwing pump is arranged at the outlet of the oil throwing tank.

Preferably, a pumping pump is arranged on the wax oil pumping pipe.

Preferably, the wax oil extraction pipe is connected to a wax oil extraction line through which a part of the wax oil can be extracted.

Preferably, a valve bank is arranged on the return line at the upper part of the wax oil, and the oil throwing tank is connected with the valve bank through a wax oil valve.

The working principle and the process are as follows:

the reaction oil gas line from the delayed coking coke tower enters a delayed coking fractionating tower and flows upwards, the wax oil collected in the wax oil collecting tank is pumped out by a wax oil pumping pipe under the action of a pumping pump and returns to the fractionating tower on the upper part of the wax oil collecting tank through a return line on the upper part of the wax oil, the condensed oil generated by preheating the coke tower of the delayed coking device is collected into an oil throwing tank, the coke tower preheats an oil throwing stage, the condensed water is removed from an emptying tower through an emptying valve in the early stage of oil throwing (before the bottom temperature of the coke tower is 180 ℃), the condensed oil in the oil throwing tank is changed to the return line on the upper part of the wax oil of the fractionating tower after the bottom temperature of the coke tower exceeds 180 ℃, and the condensed oil enters a wax oil collecting tank of the.

Compared with the prior art, the beneficial effects of the utility model are as follows:

when the coke tower is preheated to throw oil, the condensed oil does not directly enter the bottom of the fractionating tower, so that the increase of the operation circulation ratio of the device is avoided, the handling capacity of fresh feeding is ensured, and the amount of the remilled wax oil can be reduced by 20-30t in each production period according to the collection of actual operation data; meanwhile, the wax oil collecting tank is improved by throwing the wax oil, so that the yield of the wax oil of the device is increased, and the delivery amount of the wax oil is increased by 30-40t in each production period. Not only can reduce the circulation ratio, but also can increase the yield of wax oil.

Drawings

Fig. 1 is a schematic structural view of the present invention;

in the figure: 1. throwing the oil tank; 2. an oil throwing pump; 3. an atmospheric valve; 4. emptying the tower; 5. a wax oil valve; 6. a wax oil production line; 7. returning the upper part of the wax oil to the line; 8. a valve block; 9. a pump for pumping out; 10. a wax oil collection tank; 11. a reaction oil-gas line; 12. a fractionating column; 13. wax oil sump tank.

Detailed Description

The present invention will be further described with reference to the accompanying drawings.

As shown in fig. 1, the system for treating condensed oil in the preheating and oil-throwing stage of the coke tower of the delayed coking device comprises an oil-throwing tank 1 and a fractionating tower 12, wherein the fractionating tower 12 is connected with a reaction oil gas line 11, a wax oil collecting tank 13 is arranged in the fractionating tower 12, the wax oil collecting tank 13 is connected with a wax oil extracting pipe 10, the wax oil extracting pipe 10 is provided with an extracting pump 9, the wax oil extracting pipe 10 is connected with a wax oil extracting line 6, the wax oil extracting pipe 10 is connected with the fractionating tower 12 on the upper part of the wax oil collecting tank 13 through a wax oil upper part return line 7, the wax oil upper part return line 7 is provided with a valve group 8, the oil-throwing tank 1 is connected with an emptying tower 4 through an emptying valve 3, the oil-throwing tank 1 is connected with the valve group 8 on the wax oil upper part return line 7 through a wax oil valve 5.

When the device works, a reaction oil-gas line 11 from a delayed coking coke tower enters a delayed coking fractionating tower 12 and flows upwards, wax oil collected in a wax oil collecting tank 13 is pumped out by a wax oil pumping pipe 10 under the action of a pumping pump 9 and returns to the fractionating tower 12 on the upper part of the wax oil collecting tank 13 through a wax oil upper part return line 7, condensed oil generated by preheating of a coke tower of a delayed coking device is collected into an oil throwing tank 1, the condensed oil in the oil throwing tank 1 enters an emptying tower 4 through an emptying valve 3 to remove condensed water in the preheating oil throwing stage of the coke tower at the early stage of oil throwing (before the bottom temperature of the coke tower is 180 ℃), the condensed oil in the oil throwing tank 1 is changed to the wax oil upper part return line 7 of the fractionating tower 12 under the action of an oil throwing pump 2, and the condensed oil in the oil throwing tank 1 enters the wax oil collecting tank 13 of the fractionating tower 12 along with the returned wax oil.

Of course, the above description is only a preferred embodiment of the present invention, and should not be taken as limiting the scope of the embodiments of the present invention. The present invention is not limited to the above examples, and the technical field of the present invention is equivalent to the changes and improvements made in the actual range of the present invention, which should be attributed to the patent coverage of the present invention.

Claims

1. The utility model provides a processing system of oil phase condensate is got rid of in preheating of delayed coker coke drum, includes oil throwing jar (1) and fractionating tower (12), its characterized in that: the fractionating tower (12) is connected with the reaction oil gas line (11), a wax oil collecting tank (13) is arranged in the fractionating tower (12), the wax oil collecting tank (13) is connected with a wax oil extraction pipe (10), the wax oil extraction pipe (10) is connected with the fractionating tower (12) on the upper part of the wax oil collecting tank (13) through a wax oil upper part return line (7), the oil throwing tank (1) is connected with the emptying tower (4) through an emptying valve (3), and the oil throwing tank (1) is connected with the wax oil upper part return line (7) through a wax oil valve (5).

2. The system of claim 1, wherein the system further comprises: an oil throwing pump (2) is arranged at the outlet of the oil throwing tank (1).

3. The system of claim 1, wherein the system further comprises: a pump (9) is arranged on the wax oil extraction pipe (10).

4. The system of claim 1, wherein the system further comprises: the wax oil extraction pipe (10) is connected with a wax oil extraction line (6).

5. The system of claim 1, wherein the system further comprises: a valve group (8) is arranged on the return line (7) at the upper part of the wax oil, and the oil throwing tank (1) is connected with the valve group (8) through a wax oil valve (5).