CN111704521B - Quenching treatment system and quenching treatment method for olefin reaction product - Google Patents
Quenching treatment system and quenching treatment method for olefin reaction product Download PDFInfo
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- CN111704521B CN111704521B CN202010574873.9A CN202010574873A CN111704521B CN 111704521 B CN111704521 B CN 111704521B CN 202010574873 A CN202010574873 A CN 202010574873A CN 111704521 B CN111704521 B CN 111704521B
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- C07—ORGANIC CHEMISTRY
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- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
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- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
Abstract
The invention belongs to the technical field of petrochemical industry, and particularly relates to a quenching treatment system and a quenching treatment method for an olefin reaction product. The processing system comprises: a reactor (R-01), an oil gas pre-quenching tower (C-01), and a main fractionating tower (C-02); an overhead discharge line S1 of the reactor (R-01) is used as a bottom feed line of the oil gas pre-quenching tower (C-01); an overhead discharge line S2 of the oil and gas pre-quenching tower (C-01) is used as a first feed line at the bottom of the main fractionating tower (C-02), and a kettle discharge line S3 of the oil and gas pre-quenching tower (C-01) is used as a second feed line at the bottom of the main fractionating tower (C-02); the first outlet line S4 at the bottom of the main fractionator (C-02) is returned to the oil gas pre-quench tower (C-01). The invention has the creativity that the oil gas pre-quenching tower is adopted to rapidly cool the process gas, thereby improving the occurrence of coking reaction in the subsequent treatment process of the process gas and the frequent shutdown phenomenon of the device caused by coking.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a quenching treatment system and a quenching treatment method for an olefin reaction product.
Background
Olefins are important basic feedstocks for most intermediate and end products of the petroleum and chemical industries, and have an important strategic position in the development of national economy. In 2010, the ethylene capacity of China is 1519 ten thousand tons/year, and the yield is 1419 ten thousand tons/year. In 2014, the ethylene capacity breaks through 2000 ten thousand tons/year and reaches 2055.5 ten thousand tons/year. The ethylene capacity is expected to reach 3700 ten thousand tons/year in 2020.
Steam cracking is the most important process for producing ethylene and propylene at home and abroad at present, a tubular cracking furnace is adopted, no catalyst participates in the reaction process, and C in the product1、C2More by-products of propylene are produced, the industrialization is earlier, the technology is mature, and the application is wide. Because the oil and gas resource structures and the quality of all regions of the world are different, the ethylene raw material composition presents the regionalization characteristic. Asian and western european producers mainly use liquid feedstocks such as naphtha, while the middle east and north america have a greater proportion of ethane in the cracking feedstock due to the resource advantages of natural gas or shale gas associated liquids (NGL). However, the steam cracking technology has many defects, the energy consumption is high due to high reaction temperature and large steam consumption, the yield of low-value products is high, the coke of a furnace tube is quickly coked, a cracking furnace standby table is required for alternately switching coke burning, and the investment is high. The propylene/ethylene yield ratio (P/E ratio) is limited by the nature of the feedstock, is generally low, and is difficult to flexibly adjust due to the free radical reaction mechanism. Research and development of steam cracking alternative or complementary process technology has been a hotspot in the industry for many years, and can be generally divided into two technical routes, one is a low-carbon olefin production process derived from heavy oil serving as a raw material by virtue of mature experience of catalytic cracking, the other is a process for producing low-carbon olefins by taking coal (methanol) as a raw material, and industrial application is realized.
Under the current situation that the price of crude oil is continuously low and lingers, the profitability of a coal-based low-carbon olefin production line such as coal (methanol) is inhibited, and meanwhile, the coal-based raw material production line also faces multiple pressures of high one-time investment, high financing difficulty, water resource and carbon emission bearing and the like. The production of low-carbon olefin by catalytic cracking of heavy oil as a raw material has low yield of target products, which means that the primary processing capacity of crude oil needs to be enlarged, and the surplus of gasoline and diesel oil products and difficulty in sale are aggravated. And the naphtha produced olefin has a larger optimization space integrating low cost, diversification and refining of raw materials, and is beneficial to improving the overall economic benefit and market competitiveness of refining enterprises.
At present, a domestic first set of light oil catalytic cracking device for preparing low-carbon olefins starts to operate, and plays a significant role in the whole plant flow by depending on the superior oil and gas resource advantages and the oil refining processing capacity of an enterprise. The adopted process technology has the advantages of high diene yield, low energy consumption, investment saving and the like. However, the device is the first commercial industrial device in the world adopting the process technology, the practical experience of all aspects is insufficient, and the problem which is or is not expected to occur is inevitable. After the device is started, the reaction oil gas quenching heat exchanger is seriously coked, the outlet temperature is increased to 500 ℃ in a short time (30-40 days), the shutdown and decoking treatment has to be carried out for ensuring safety under the limitation of the original design conditions of related pipelines and equipment, and the frequent start and stop seriously affects the economic benefits of the device and the whole plant.
The subsequent treatment of the catalytic cracking reaction products currently has only one mode: the reaction product is heat exchanged in a heat exchanger and then enters a main fractionating tower to separate fractions. Another treatment method in a catalytic cracking unit for oil refining: the reaction product directly enters a main fractionating tower to separate each fraction. Aiming at the reaction of preparing low-carbon olefin by catalytic cracking, the temperature of the catalytic cracking reaction product is generally as high as 500-700 ℃, and the components of the reaction product are complex, for example, condensation reaction can occur at high temperature of aromatic hydrocarbon, and polymerization reaction can occur to olefin, so that coking phenomenon can occur. For the reaction generated by the substances easy to coke, if a first treatment mode is adopted, the reaction product is subjected to heat exchange through a heat exchanger, the coking reaction can occur in a heat exchanger pipeline, the heat exchanger pipeline can be blocked, and shutdown and coke cleaning treatment needs to be carried out regularly; if the second treatment mode is adopted, the reaction product directly enters the main fractionating tower, and the high-temperature reaction product continuously generates side reaction in a longer pipeline, then coking reaction can occur in the pipeline and the main fractionating tower, the coking product can be deposited in the pipeline and the tower kettle of the main fractionating tower and partially mixed with kettle liquid, the tower kettle also needs to be cleaned and the separation kettle liquid needs to be treated, and in addition, the side reaction can also cause the loss of ethylene and propylene products.
Under the background, the quenching system for preparing olefin oil gas by catalytic cracking needs to be improved and optimized.
Disclosure of Invention
The present invention has been made to solve the above problems. The invention aims to provide a high-efficiency olefin reaction product quenching treatment system and a quenching treatment method, which realize long-period high-efficiency operation of the whole device, reduce energy consumption and improve the economic benefit of the device by carrying out direct oil quenching on high-temperature process gas of a reaction product, using a quenching oil steam generator as a heat source in the device and the like.
The invention provides an olefin reaction product quenching treatment system in a first aspect, which comprises the following devices: a reactor R-01, an oil gas pre-quenching tower C-01 and a main fractionating tower C-02;
the connection relationship among the devices is as follows:
the top discharge line S1 of the reactor R-01 is used as a bottom feed line of the oil gas pre-quenching tower C-01;
an overhead discharge line S2 of the oil and gas pre-quenching tower C-01 serves as a first bottom feed line of the main fractionating tower C-02, and a kettle discharge line S3 of the oil and gas pre-quenching tower C-01 serves as a second bottom feed line of the main fractionating tower C-02;
the first bottom discharge line S4 of the main fractionator C-02 is returned to the oil and gas pre-quench tower C-01 and is divided into two paths, one of which is introduced into the oil and gas pre-quench tower C-01 from the middle as a first side feed S5, and the other is introduced into the oil and gas pre-quench tower C-01 from the top as a second top feed S6.
The reactor R-01 is a reactor for preparing olefin by catalytic cracking.
The main fractionating tower C-02 is a quenching oil tower.
Preferably, the treatment system further comprises a cooling spray nozzle Q-01 disposed on the overhead discharge line S1;
the first discharge pipeline S4 at the bottom of the main fractionating tower C-02 is divided into three paths, wherein the two paths are respectively the first feed pipeline S5 at the side line and the second feed pipeline S6 at the top of the main fractionating tower C-02, and the third path is a cooling spray nozzle quenching oil feed pipeline S11 communicated with the cooling spray nozzle Q-01.
Preferably, the processing system further comprises the following means: an oil slurry filter S-01 and heat exchange equipment;
the connection relationship among the devices is as follows:
the oil slurry filter S-01 and the heat exchange equipment are arranged at the downstream of the main fractionating tower C-02;
the top of the main fractionating tower C-02 is connected with an oil washing process gas extraction pipeline S10, and the bottom of the main fractionating tower C-02 is connected with a second discharge circulating pipeline S7 and a third discharge circulating pipeline S8;
the second discharge circulation pipeline S7 is divided into two paths, wherein one path returns to the main fractionating tower C-02 after passing through the slurry oil filter S-01 to be used as a third feed pipeline S9 at the bottom of the main fractionating tower C-02, and the other path is directly used as a self-produced fuel oil extraction pipeline S12;
the third discharge circulation line S8 is returned to the main fractionator C-02 after passing through the heat exchange device.
Preferably, the cooling spray head Q-01 is provided with a plurality of quenching oil spray nozzles which are uniformly and symmetrically distributed along the cooling spray head Q-01 in an annular shape;
and a plurality of layers of trays are designed in the oil gas pre-quenching tower C-01.
The specific structure of the reactor R-01, the tower, the filter and the heat exchange equipment can be selected from the conventional design in the field.
The reactor R-01 is used for carrying out the reaction of preparing olefin by catalytic cracking, and the specific design of the reactor R-01 and the specific reaction carried out in the reactor can refer to the prior art in the field. The invention only aims at the subsequent quenching treatment of the reaction product. The main fractionating tower C-02 is used for separating reaction products of the reaction for preparing olefin by catalytic cracking, and the specific design and operation parameters of the main fractionating tower C-02 can refer to the prior art in the field.
In the present invention, "quenching" means: the reaction product is cooled to below 400 ℃ in as short a time as possible, with faster cooling resulting in less side reactions.
The main column C-02 is used for: and (3) fractionating the mixture in the tower to mainly separate the following three sections: oil washing process gas (mainly containing H)2C1-C4, light gasoline component, CO2Iso acid gas) A heavy gasoline component, and a diesel component.
The second aspect of the present invention provides a quenching treatment method for an olefin reaction product, using the quenching treatment system of the first aspect of the present invention, the quenching treatment method comprising the following steps:
the reactor R-01 is used for catalytic cracking reaction for preparing olefin, the reaction product is a process gas containing olefin, and the process gas contains C1-C10 hydrocarbon fraction containing ethylene and propylene, hydrogen and CO2Waiting for acid gas at the temperature of 550-700 ℃;
adding circulating gasoline as quenching gasoline into the main fractionating tower C-02;
the process gas enters the oil gas pre-quenching tower C-01 through the top discharge line S1 of the reactor R-01, contacts with quenching oil introduced by the main fractionating tower C-02 through a first feeding pipe S5 and a top second feeding pipe S6 in the oil gas pre-quenching tower C-01, is cooled to 400 ℃, and enters the main fractionating tower C-02 from the top discharge line S2;
and the process gas is contacted and cooled again by the quenching oil and is fractionated to separate the oil-washed process gas, the heavy gasoline distillate oil and the diesel oil distillate oil.
The temperature of the oil washing process gas extracted from the tower top is 101-110 ℃.
Preferably, the process gas is cooled by the quenching oil injected by the cooling nozzle Q-01 before entering the oil gas pre-quenching tower C-01.
The principle of the invention is as follows: the oil gas pre-quenching tower is adopted to rapidly cool the process gas, and substances easy to coke do not generate cracking and condensation reaction due to high temperature, so that the process relieves the occurrence of coking reaction in the subsequent treatment process of the process gas.
The technical scheme can be freely combined on the premise of no contradiction.
The invention has the following beneficial effects:
1. in the reaction of preparing olefin by catalytic cracking, coking reaction is always a difficult problem which troubles the technical personnel in the field. In the prior art, the heat exchanger is generally subjected to decoking treatment regularly, or a reaction product is directly introduced into a main fractionating tower to treat a coking product in a main fractionating tower kettle, so that more side reactions are caused, and coking is aggravated. The invention firstly arranges an oil gas pre-quenching tower between the catalytic cracking reactor and the main fractionating tower, and the oil gas pre-quenching tower rapidly cools the process gas with the reactor outlet temperature of 550-700 ℃ to 320-400 ℃ and then enters the main fractionating tower for cooling and fractionating. The treatment system and the method designed by the invention slow down the coking reaction of the high-temperature process gas. The invention has the creativity that the process gas is rapidly cooled by adopting an oil gas pre-quenching tower instead of the purpose of quenching and heat exchange in the prior art (the heat exchanger is mainly used for recovering heat in the prior art), the substances easy to coke do not generate cracking and condensation reaction due to high temperature, and the process relieves the occurrence of coking reaction in the subsequent treatment process of the process gas.
2. When the process gas is cooled in the pipeline, for example, the process gas is cooled by a heat exchanger or is cooled by a cooling spray head arranged on the pipeline, gas-liquid two-phase separation cannot be realized, and the gas-liquid two-phase occurs in the pipeline. The gas-liquid two-phase flow has large impact force on the pipeline, the flow is unstable, the vibration is easily caused, and the pipeline and the equipment are damaged. The oil gas pre-quenching tower rapidly cools the process gas with the temperature of 550-700 ℃ at the outlet of the reactor to 320-400 ℃, realizes gas-liquid phase separation and avoids the condition of gas-liquid two-phase flow in a pipeline.
3. The invention arranges an oil gas pre-quenching tower between the catalytic cracking reactor and the main fractionating tower to rapidly cool the process gas, thereby reducing the cooling load of the main fractionating tower.
Drawings
FIG. 1 is a flow diagram of a quenching treatment system for olefin reaction products of example 1.
List of reference numerals:
r-01, a reactor, Q-02, a cooling spray nozzle, C-01, an oil gas pre-quenching tower, C-02, a main fractionating tower, P-01, a quenching oil circulating pump, P-02, a fuel oil pump, S-01, an oil slurry filter, E-01, a quenching oil heat exchanger, E-02 and a quenching oil steam generator.
Detailed Description
The present invention will be further described with reference to the following embodiments.
Example 1
As shown in fig. 1, a quenching treatment system for olefin reaction products comprises the following devices:
the system comprises a reactor R-01, a cooling spray nozzle Q-01, an oil gas pre-quenching tower C-01, a main fractionating tower C-02, an oil slurry filter S-01, heat exchange equipment, a quenching oil circulating pump P-01, a fuel oil pump P-02 and a valve V1;
the connection relationship among the devices is as follows:
a reaction feed line S0 is used as a feed line of the reactor R-01, and an overhead discharge line S1 of the reactor R-01 is used as a bottom feed line of the oil gas pre-quenching tower C-01;
the cooling spray nozzle Q-01 is arranged on the top discharge pipeline S1, and the cooling spray nozzle Q-01 is provided with a plurality of quenching oil spray nozzles which are uniformly and symmetrically distributed along the cooling spray nozzle Q-01 in an annular shape.
The cooling spray head Q-01 and the cooling spray head quenching oil feeding pipeline S11 are communicated with a steam pipeline S14, and a flow limiting orifice plate is arranged on the steam pipeline S14. A valve V1 is provided on the steam line S14. The steam pipeline S14 is introduced with back-flushing steam, when the quenching oil suddenly has no flow, the back-flushing steam is opened by quickly cutting off the valve V1 to avoid the oil gas from flowing backwards, and the design capability of the cooling spray head Q-01 is to quench the process gas at 700 ℃ to 320-400 ℃;
an overhead discharge line S2 of the oil and gas pre-quenching tower C-01 serves as a first bottom feed line of the main fractionating tower C-02, and a kettle discharge line S3 of the oil and gas pre-quenching tower C-01 serves as a second bottom feed line of the main fractionating tower C-02;
the first discharge pipeline S4 at the bottom of the main fractionating tower C-02 is divided into three paths, wherein the two paths return to the oil gas pre-quenching tower C-01, the first path enters the oil gas pre-quenching tower C-01 from a tower middle tray as a side line first feed pipe S5, the second path enters the oil gas pre-quenching tower C-01 from the top as a tower top second feed pipe S6, and the third path is a cooling spray head quenching oil feed pipeline S11 communicated with the cooling spray head Q-01, the top of the main fractionating tower C-02 is connected with an oil-washing process gas extraction pipeline S10, the bottom of the main fractionating tower C-02 is connected with a second discharge circulating pipeline S7 and a third discharge circulating pipeline S8, a circulating gasoline pipeline S16 is communicated with the top of the main fractionating tower C-02, and the middle part of the main fractionating tower C-02 is connected with a heavy gasoline pipeline S17;
a fuel oil pump P-02 is arranged on the second discharging circulating pipeline S7, the second discharging circulating pipeline S7 is divided into two paths, one path of the two paths of the oil slurry filters S12 are respectively taken are taken as self-production fuel oil filters S3535;
the third discharging circulation line S8 returns to the main fractionating tower C-02 after passing through the heat exchange device, and a quenching oil circulation pump P-01 is arranged on the third discharging circulation line S8.
The oil gas pre-quenching tower C-01 is communicated with a steam pipeline S13. 4 layers of chimney trays are designed in the oil gas pre-quenching tower C-01. In addition, in other embodiments, trays of the oil-gas pre-quenching tower C-01 can be designed according to calculation conditions, and 4-8 chimney trays or large-sieve-hole trays are usually arranged for better gas-liquid phase mass transfer and heat transfer.
The heat exchange device comprises a plurality of quenching oil heat exchangers E-01 connected in series and a quenching oil steam generator E-02 connected with the quenching oil heat exchangers in parallel.
For the new project, only the oil gas pre-quenching tower C-01 can be designed, the oil gas pre-quenching tower C-01 is arranged at the top of the reactor R-01, and the process gas from the reactor enters the oil gas pre-quenching tower upwards in the shortest distance.
If the oil gas pre-quenching tower C-01 cannot be directly arranged at the top of the reactor R-01 or in a modification device, a cooling spray nozzle Q-01 and the oil gas pre-quenching tower C-01 can be simultaneously adopted, or only the oil gas pre-quenching tower C-01 is adopted. Partial quenching is carried out through the cooling spray nozzle Q-01, so that the pipeline stress of the high-temperature quenching pipeline can be reduced, and the investment is saved. The quenching amount of the cooling spray head Q-01 and the quenching amount of the oil gas pre-quenching tower C-01 can be designed according to the capability of cooling a reaction product to 320-400 ℃ by using two quenching methods, and in actual operation, the loads of the two quenching methods can be distributed according to the field conditions. The cooling spray Q-01 is arranged on a vertical pipe as close as possible to the reactor R-01 to save space.
In both quenching methods, a regulating valve is designed on a quenching oil pipeline, and the purpose is to control the temperature of the process gas after quenching by direct contact of quenching oil within a temperature range of 320-400 ℃.
The structural design and the specific installation mode of the steam pipeline and the heat exchange equipment belong to the common knowledge in the field.
Example 2
A quenching treatment method for an olefin reaction product, using the quenching treatment system according to the first aspect of the invention, the quenching treatment method comprising the steps of:
raw oil enters the reactor R-01 through the reaction feed pipeline S0 to undergo catalytic cracking reaction, the reaction product is a process gas containing olefin, and the process gas contains C containing ethylene and propylene1～C10Hydrocarbon fraction, hydrogen, CO2Waiting for acid gas at the temperature of 550-700 ℃;
adding circulating gasoline as quenching oil into the main fractionating tower C-02;
and (3) the olefin reaction product process gas coming out of the top of the reactor R-01 is at the temperature of 550-700 ℃, carries a small amount of catalyst particles, enters the cooling spray nozzle Q-01 through the reaction feed line S1, and is mixed with quenching oil and quenched in the cooling spray nozzle Q-01. Quenching oil enters the reaction feed pipeline S1 through a plurality of annular quenching oil nozzles which are uniformly and symmetrically distributed on the cooling spray head quenching oil feed pipeline S11 and the cooling spray head Q-01, and the flow rate of the quenching oil of each nozzle is controlled at 0-30 t/hr. To ensure uniform distribution, an annular distributor is designed at the cooling spray head quench oil feed line S11, and quench oil is drawn from the top of the annular distributor and then injected into the quench oil nozzles from top to bottom.
Every nozzle all designs corresponding steam line all the way, and its steam line from the bottom up injects into quench oil nozzle annulus to play the coking prevention and prevent stifled, play the atomizing simultaneously the effect of quench oil. And the steam pipeline S14 is filled with back-blowing steam, and when the quenching oil suddenly has no flow, the valve V1 is quickly cut off, the back-blowing steam is opened, and the oil gas is prevented from flowing backwards. The cooling showerhead Q-01 is designed to quench process gas at 700 degrees Celsius to 320 and 400 degrees Celsius. In practical use, the cooling temperature of the cooling spray nozzle Q-01 and the cooling temperature of the oil gas pre-quenching tower C-01 can be flexibly controlled. So that the temperature of the process gas after passing through the cooling spray nozzle Q-01 and the oil gas pre-quenching tower C-01 is 320-400 ℃.
The cooling spray nozzle Q-01 and the oil gas pre-quenching tower C-01 are close to each other as much as possible. And the process gas passing through the cooling spray nozzle Q-01 is sent into the oil gas pre-quenching tower C-01, and the process gas is contacted and cooled with quenching oil from top to bottom in the tower. The quenching oil input from the first outlet line S4 at the bottom of the main fractionating tower C-02 is injected into the oil gas pre-quenching tower C-01 in two ways, one way enters the oil gas pre-quenching tower C-01 from the middle part through the first inlet pipe S5 at the side, the other way enters the oil gas pre-quenching tower C-01 from the upper part through the second inlet pipe S6 at the top of the tower, and the ratio of the quenching oil at the upper part to the quenching oil at the middle part is 1:1 to 2: 1. The flow rate of the quenching oil is controlled by the temperature of the quenching process gas at the top of the oil gas pre-quenching tower C-01.
And introducing low-pressure steam into the bottom of the oil gas pre-quenching tower C-01 through a steam pipeline S13, wherein the low-pressure steam plays a role in stripping and stirring. Meanwhile, a fire-fighting steam is designed to be communicated to the outer bottom of the oil gas pre-quenching tower C-01 tank for fire extinguishing in emergency.
The temperature of the process gas after quenching and cooling through the oil gas pre-quenching tower C-01 is controlled to be 320-400 ℃, and the process gas enters the bottom of the main fractionating tower C-02 after leaving from the oil gas pre-quenching tower C-01. In the quenching process, part of unvaporized quenching oil is fed into the main fractionating tower C-02 from the bottom of the oil-gas pre-quenching tower C-01 through a tower bottom discharge pipeline S3, so that the recycling of the quenching oil is realized.
And the process gas enters the main fractionating tower C-02 to realize further cooling, the process gas is contacted with circulating quenching oil in the process and then contacted with circulating gasoline introduced by the circulating gasoline pipeline S16, and finally the temperature of the oil-washed process gas extracted by the oil-washed process gas extraction pipeline S10 is 101-110 ℃.
And introducing steam at the bottom of the main fractionating tower C-02 as stripping steam and stirring steam to avoid accumulation of bottom coke. The bottom oil and bottom oil components of the main fractionating tower C-02 are as follows: a part of the quenching oil and the solid particles is filtered and returned to the main fractionating tower C-02 through the slurry oil filter S-01 so as to reduce the deposition of the solid particles in the main fractionating tower C-02. The solid particles are derived from small amounts of catalyst and coked particulate carried in the process gas. The other part of the bottom oil at the bottom of the main fractionating tower C-02 is taken out as self-produced fuel oil which can be used as device fuel, for example, the self-produced fuel oil is introduced into a catalyst regeneration section of a reactor to provide heat for the reaction. The middle portion of the main fractionator C-02 extracts heavy gasoline components through the heavy gasoline line S17.
It should be noted that: the specific composition of the process gas in each apparatus or line is not exactly the same.
The specific flows in each pipeline are as follows:
reaction feed line S0: light distillate oil.
Reactor knockout line S1: process gas (C containing ethylene propylene)1～C10Hydrocarbon fraction, hydrogen, CO2Etc., acid gases), a small amount of catalyst particles. Temperature: 550-700 degrees celsius.
Overhead discharge line S2: process gas (C containing ethylene propylene)1～C10Hydrocarbon fraction, hydrogen, CO2Acid gases, etc.), water vapor. Temperature: 320-400 deg.c.
Column bottom discharge line S3: quenching oil and a small amount of catalyst particles.
Bottom first discharge line S4: quenching oil.
Side line first feeding pipe S5: quenching oil.
Second overhead feed line S6: quenching oil.
Second effluent circulating line S7: quench oil (containing a small amount of solid particles).
Third effluent circulation line S8: the components are the same as S7.
Bottom third feed line S9: and (5) filtering the quenching oil.
Oil wash process gas production line S10: oil washing process gas (mainly containing H)2C1-C4, light gasoline component, CO2Equal acid gas), water vapor, temperature: 101 deg.c and 110 deg.c.
The self-produced fuel oil production line S12: self-produced fuel oil (diesel and above fractions).
Cooling spray nozzle quench oil feed line S11: quenching oil.
Steam line S14: and (4) water vapor.
Steam line S13: and (4) water vapor.
Circulating gasoline line S16: quenching the gasoline.
Heavy gasoline line S17: a heavy gasoline component.
The quenching oil of the invention is mainly diesel oil and fractions above.
Example 3
This example provides a quenching treatment system and a quenching treatment method for olefin reaction products, and the flow chart is shown in fig. 1.
In the embodiment, the main flow is similar to that of embodiment 1, the cooling spray nozzle Q-01 is adopted to directly cool the olefin reaction product to 320-400 ℃, the oil-gas pre-quenching tower C-01 does not carry out quenching on the process gas, and the oil-gas pre-quenching tower C-01 is used for separating gas-liquid two phases, wherein the gas phase is sent into the main fractionating tower C-02 from the top of the oil-gas pre-quenching tower C-01, and the liquid phase is sent into the main fractionating tower C-02 from the bottom of the oil-gas pre-quenching tower C-01.
Example 4
The embodiment provides a quenching treatment system and a quenching treatment method for an olefin reaction product.
The main flow and method of this example are similar to example 1, except that: cooling by a cooling spray nozzle Q-01 is not adopted, namely the cooling spray nozzle Q-01 is not arranged on the discharge pipeline S1 at the top of the tower. In this case, the oil and gas pre-quenching tower C-01 may be directly disposed at the top of the reactor R-01. In the oil gas pre-quenching tower C-01, cooling the process gas from 550-700 ℃ to 320-400 ℃. After cooling, the gas phase material in the process gas and the quenching oil is sent to the main fractionating tower C-02 from the top of the oil gas pre-quenching tower C-01, and the liquid phase material is sent to the main fractionating tower C-02 from the bottom of the oil gas pre-quenching tower C-01.
Comparative example 1
And replacing the cooling spray head and the oil gas pre-quenching tower C-01 with a quenching heat exchanger. After the device is started, the quenching heat exchanger is seriously coked, the outlet temperature is increased to 500 ℃ in a short time (30-40 days), and the shutdown and decoking treatment has to be frequently carried out to ensure safety under the limitation of the original design conditions of related pipelines and equipment.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (3)
1. An olefin reaction product quenching treatment system, which is characterized by comprising the following devices: a reactor (R-01), an oil gas pre-quenching tower (C-01), and a main fractionating tower (C-02);
the connection relationship among the devices is as follows:
an overhead discharge line S1 of the reactor (R-01) is used as a bottom feed line of the oil gas pre-quenching tower (C-01);
an overhead discharge line S2 of the oil and gas pre-quenching tower (C-01) is used as a first feed line at the bottom of the main fractionating tower (C-02), and a kettle discharge line S3 of the oil and gas pre-quenching tower (C-01) is used as a second feed line at the bottom of the main fractionating tower (C-02);
the bottom first discharge line S4 of the main fractionator (C-02) is returned to the oil and gas pre-quench tower (C-01) and is divided into two paths, one of which is introduced into the oil and gas pre-quench tower (C-01) from the middle as a side first feed S5, and the other is introduced into the oil and gas pre-quench tower (C-01) from the top as an overhead second feed S6;
the treatment system further comprises a cooling spray head (Q-01) disposed on the overhead discharge line S1;
the first discharge pipeline S4 at the bottom of the main fractionating tower (C-02) is divided into three paths, wherein the two paths are respectively the first feed pipeline S5 at the side line and the second feed pipeline S6 at the top of the main fractionating tower, and the third path is a cooling spray nozzle quenching oil feed pipeline S11 communicated with the cooling spray nozzle (Q-01);
the processing system further comprises the following means: an oil slurry filter (S-01), heat exchange equipment;
the connection relationship among the devices is as follows:
said slurry filter (S-01) and heat exchange means are arranged downstream of said main fractionation column (C-02);
the top of the main fractionating tower (C-02) is connected with an oil washing process gas extraction line S10, and the bottom of the main fractionating tower (C-02) is connected with a second discharge circulating line S7 and a third discharge circulating line S8;
the second discharge circulation pipeline S7 is divided into two paths, wherein one path returns to the main fractionating tower (C-02) as a third feeding pipeline S9 at the bottom of the main fractionating tower after passing through the slurry oil filter (S-01), and the other path is directly used as a self-produced fuel oil extraction pipeline S12;
said third effluent recycle line S8 is returned to said main fractionation column (C-02) after passing through said heat exchange means;
the cooling spray head (Q-01) is provided with a plurality of quenching oil spray nozzles which are uniformly and symmetrically distributed along the cooling spray head (Q-01) in an annular shape;
a plurality of layers of tower trays are designed in the oil gas pre-quenching tower (C-01);
and each path of nozzle is provided with a corresponding steam pipeline, and the steam pipeline is injected into the quenching oil nozzle annular space from bottom to top.
2. A quenching treatment method for olefin reaction products, which is characterized in that the quenching treatment system of claim 1 is used, and the quenching treatment method comprises the following steps:
the reactor (R-01) is used for carrying out catalytic cracking reaction for preparing olefin, the reaction product is a process gas containing olefin, and the process gas contains C containing ethylene and propylene1～C10Hydrocarbon fraction, hydrogen and acid gas at 550-700 ℃;
adding circulating gasoline as quenching gasoline into the main fractionating tower (C-02);
the process gas enters the oil gas pre-quenching tower (C-01) through the top discharge line S1 of the reactor (R-01), contacts with quenching oil introduced by the main fractionating tower (C-02) through the side line first feed pipe S5 and the top second feed pipe S6 in the oil gas pre-quenching tower (C-01), is cooled to the temperature of 320 ℃ and 400 ℃, and enters the main fractionating tower (C-02) from the top discharge line S2;
in the main fractionating tower (C-02), the process gas is again cooled by contact with the quench oil and fractionated to separate the oil-washed process gas, heavy gasoline distillate and diesel distillate.
3. The quenching treatment method according to claim 2, wherein the process gas is cooled by quenching oil injected by the cooling spray nozzle (Q-01) before entering the oil gas pre-quenching tower (C-01).
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1270206A (en) * | 2000-04-29 | 2000-10-18 | 中国石化集团洛阳石油化工工程公司 | Suddenly cooling tower and process of resultant from fluidized catalytic transform reaction of hydrocarbons |
| JP2006307134A (en) * | 2005-03-31 | 2006-11-09 | Mitsubishi Chemicals Corp | METHOD FOR SEPARATING C2+ FRACTION FROM NOx-CONTAINING LIGHT GAS |
| CN104837792A (en) * | 2012-10-31 | 2015-08-12 | 国际壳牌研究有限公司 | Processes for the preparation of an olefinic product |
| CN207016686U (en) * | 2017-03-15 | 2018-02-16 | 神华集团有限责任公司 | Methanol-to-olefins device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| KR100632571B1 (en) * | 2005-10-07 | 2006-10-09 | 에스케이 주식회사 | Process for the preparation of light olefins in catalytic cracking from hydrocarbon feedstock |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1270206A (en) * | 2000-04-29 | 2000-10-18 | 中国石化集团洛阳石油化工工程公司 | Suddenly cooling tower and process of resultant from fluidized catalytic transform reaction of hydrocarbons |
| JP2006307134A (en) * | 2005-03-31 | 2006-11-09 | Mitsubishi Chemicals Corp | METHOD FOR SEPARATING C2+ FRACTION FROM NOx-CONTAINING LIGHT GAS |
| CN104837792A (en) * | 2012-10-31 | 2015-08-12 | 国际壳牌研究有限公司 | Processes for the preparation of an olefinic product |
| CN207016686U (en) * | 2017-03-15 | 2018-02-16 | 神华集团有限责任公司 | Methanol-to-olefins device |
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