阅读说明：本技术 一种降低催化装置能耗的加工方法 (Processing method for reducing energy consumption of catalytic device ) 是由 陶春风 滕明才 刘海星 于 2020-07-29 设计创作，主要内容包括：本发明涉及一种降低催化装置能耗的加工方法,包括如下步骤：a、在分馏塔的外侧配备一中油--超重芳烃换热器,在解析塔的外侧配备解析塔底物料换热器,一中油--超重芳烃换热器通过管路连接分馏塔,解析塔底物料换热器通过管路与解析塔连接；b、循环超重芳烃从泵出来后首先通过一中油--超重芳烃换热器与一中油换热,取出超重芳烃的高位热能；c、被加热之后的一中油按原有工艺流程在进返塔冷却器之前先与解析塔底物料换热器中的物料换热,从而降低原解析塔底重沸器加热蒸汽的用量,工艺流程简单,布局合理,方便操作,取热效率合理,增加了公司的经济效益。(The invention relates to a processing method for reducing energy consumption of a catalytic device, which comprises the following steps: a. the outer side of the fractionating tower is provided with an intermediate oil-overweight aromatic heat exchanger, the outer side of the desorption tower is provided with a material heat exchanger at the bottom of the desorption tower, the intermediate oil-overweight aromatic heat exchanger is connected with the fractionating tower through a pipeline, and the material heat exchanger at the bottom of the desorption tower is connected with the desorption tower through a pipeline; b. after the circulating overweight aromatic hydrocarbon is pumped out, firstly, the circulating overweight aromatic hydrocarbon exchanges heat with the medium oil through a medium oil-overweight aromatic hydrocarbon heat exchanger, and the high-level heat energy of the overweight aromatic hydrocarbon is taken out; c. the heated oil in the first step exchanges heat with the material in the material heat exchanger at the bottom of the resolving tower before entering and returning to the tower cooler according to the original process flow, so that the consumption of the heating steam of the reboiler at the bottom of the original resolving tower is reduced, the process flow is simple, the layout is reasonable, the operation is convenient, the heat extraction efficiency is reasonable, and the economic benefit of a company is increased.)

1. A processing method for reducing energy consumption of a catalytic device is characterized by comprising the following steps:

a. the outer side of the fractionating tower is provided with an intermediate oil-overweight aromatic heat exchanger, the outer side of the desorption tower is provided with a material heat exchanger at the bottom of the desorption tower, the intermediate oil-overweight aromatic heat exchanger is connected with the fractionating tower through a pipeline, and the material heat exchanger at the bottom of the desorption tower is connected with the desorption tower through a pipeline;

b. after the circulating overweight aromatic hydrocarbon is pumped out, firstly, the circulating overweight aromatic hydrocarbon exchanges heat with the medium oil through a medium oil-overweight aromatic hydrocarbon heat exchanger, and the high-level heat energy of the overweight aromatic hydrocarbon is taken out;

c. the heated oil in the first step exchanges heat with the material in the material heat exchanger at the bottom of the desorption tower before entering the tower cooler according to the original process flow, thereby reducing the consumption of the heating steam of the reboiler at the bottom of the original desorption tower.

2. The process of claim 1, wherein the process parameters are controlled as follows: the bottom temperature of the fractionating tower is 320-350 ℃; a middle circulation amount of 150-230 t/h; the recycling amount of overweight aromatic hydrocarbon is 200-400 t/h; the desorption bottom temperature is 110-130 ℃.

Technical Field

The invention relates to the field of catalytic cracking oil refining processing, in particular to a processing method for reducing energy consumption of a catalytic device.

Background

Catalytic cracking is an important secondary processing technology in oil refineries, plays a positive role in the process of converting heavy crude oil into light crude oil, but consumes a large amount of energy while producing light fuel. The quality of the operation condition of the device directly influences the energy utilization level of the device, and further influences the comprehensive energy consumption and economic benefit of the oil refinery. Compared with the energy consumption of similar catalytic cracking units abroad, the energy consumption of the catalytic cracking unit in China is generally higher. When the catalytic cracking device is produced according to the designed full load, the temperature of the bottom of the fractionating tower in the catalytic fractionating system is higher than the upper limit of the control index of 350 ℃, overweight aromatic hydrocarbon at the bottom of the tower is easy to coke, the device is not favorable for the safe and stable operation of the process operation and the long period of equipment, the whole heat extraction load of the tower is large, the processing capacity of the device is not up to the standard due to the limitation, the economic benefit of an enterprise is poor, and the desorption tower in the downstream absorption stabilizing device uses 1.0MPA steam as a heat source, so that the energy consumption of the whole device is increased, and the whole economic benefit.

Disclosure of Invention

The invention aims to overcome the defects in the prior art and provide a processing method for reducing the energy consumption of a catalytic device.

In order to achieve the purpose, the technical scheme adopted by the invention is as follows:

a processing method for reducing energy consumption of a catalytic device comprises the following steps:

a. the outer side of the fractionating tower is provided with an intermediate oil-overweight aromatic heat exchanger, the outer side of the desorption tower is provided with a material heat exchanger at the bottom of the desorption tower, the intermediate oil-overweight aromatic heat exchanger is connected with the fractionating tower through a pipeline, and the material heat exchanger at the bottom of the desorption tower is connected with the desorption tower through a pipeline;

b. after the circulating overweight aromatic hydrocarbon is pumped out, firstly, the circulating overweight aromatic hydrocarbon exchanges heat with the medium oil through a medium oil-overweight aromatic hydrocarbon heat exchanger, and the high-level heat energy of the overweight aromatic hydrocarbon is taken out;

c. the heated oil in the first step exchanges heat with the material in the material heat exchanger at the bottom of the desorption tower before entering the tower cooler according to the original process flow, thereby reducing the consumption of the heating steam of the reboiler at the bottom of the original desorption tower.

Further, the process parameters are controlled as follows: the bottom temperature of the fractionating tower is 320-350 ℃; a middle circulation amount of 150-230 t/h; the recycling amount of overweight aromatic hydrocarbon is 200-400 t/h; the desorption bottom temperature is 110-130 ℃.

The invention has the beneficial effects that: this patent is on the basis of current device, add two heat exchangers and corresponding pipeline and pipe fitting, retrieve the surplus heat at the bottom of the fractionating tower, the temperature at the bottom of the control tower prevents overweight arene coking in the index from blockking up damage equipment, reduce the pressure of getting hot of upper portion middle section backward flow, provide sufficient heat for follow-up apparatus for producing simultaneously, thereby reduce the quantity of steam, energy saving and consumption reduction, the small investment, process flow is simple, rationally distributed, convenient operation, it is equitable to get thermal efficiency, company's economic benefits has been increased.

Drawings

FIG. 1 is a process flow diagram of the present invention.

Detailed Description

As shown in fig. 1, a processing method for reducing energy consumption of a catalytic device comprises the following steps:

a. the outer side of the fractionating tower is provided with an intermediate oil-overweight aromatic heat exchanger, the outer side of the desorption tower is provided with a material heat exchanger at the bottom of the desorption tower, the intermediate oil-overweight aromatic heat exchanger is connected with the fractionating tower through a pipeline, and the material heat exchanger at the bottom of the desorption tower is connected with the desorption tower through a pipeline;

b. after the circulating overweight aromatic hydrocarbon is pumped out, firstly, the circulating overweight aromatic hydrocarbon exchanges heat with the medium oil through a medium oil-overweight aromatic hydrocarbon heat exchanger, and the high-level heat energy of the overweight aromatic hydrocarbon is taken out;

c. the heated oil in the first step exchanges heat with the material in the material heat exchanger at the bottom of the desorption tower before entering the tower cooler according to the original process flow, thereby reducing the consumption of the heating steam of the reboiler at the bottom of the original desorption tower.

Further, the process parameters are controlled as follows: the bottom temperature of the fractionating tower is 320-350 ℃; a middle circulation amount of 150-230 t/h; the recycling amount of overweight aromatic hydrocarbon is 200-400 t/h; the desorption bottom temperature is 110-130 ℃.

This patent is on the basis of current device, add two heat exchangers and corresponding pipeline and pipe fitting, retrieve the surplus heat at the bottom of the fractionating tower, the temperature at the bottom of the control tower prevents overweight arene coking in the index from blockking up damage equipment, reduce the pressure of getting hot of upper portion middle section backward flow, provide sufficient heat for follow-up apparatus for producing simultaneously, thereby reduce the quantity of steam, energy saving and consumption reduction, the small investment, process flow is simple, rationally distributed, convenient operation, it is equitable to get thermal efficiency, company's economic benefits has been increased.

The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are merely illustrative of the principles of the invention, but that various changes and modifications may be made without departing from the spirit and scope of the invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.