CN111019688B

CN111019688B - Low-carbon olefin cracking equipment and cracking method

Info

Publication number: CN111019688B
Application number: CN201811177455.5A
Authority: CN
Inventors: 张利军; 周丛; 李蔚; 王国清; 石莹; 张兆斌; 刘俊杰
Original assignee: Sinopec Beijing Research Institute of Chemical Industry; China Petroleum and Chemical Corp
Current assignee: Sinopec Beijing Research Institute of Chemical Industry; China Petroleum and Chemical Corp
Priority date: 2018-10-10
Filing date: 2018-10-10
Publication date: 2022-03-15
Anticipated expiration: 2038-10-10
Also published as: CN111019688A

Abstract

The invention relates to the field of petroleum cracking, and discloses a low-carbon olefin cracking device and a cracking method. The low-carbon olefin cracking equipment comprises a convection section (2), a radiation section (5), a quenching boiler (6), a separation tower (8) and a pressure reducing device (10) which are sequentially communicated, wherein the pressure reducing device enables pipelines of materials flowing through the convection section (2), the radiation section (5), the quenching boiler (6) and the separation tower (8) to be in a negative pressure state, and the radiation section (5) comprises a hearth, a furnace wall (11) arranged on the inner wall of the hearth, at least one tube bundle (3) arranged inside the hearth and a plurality of burners (4) arranged on the side wall and/or the bottom wall of the hearth. The invention uses the pressure reducing device to make the pipelines of the convection section, the radiation section and the quenching boiler flowing through the materials in a negative pressure state, the heavy cracking raw material can be fully gasified in the convection section, the process cost can be saved, and the coking of the cracking furnace can be effectively reduced.

Description

Low-carbon olefin cracking equipment and cracking method

Technical Field

The invention relates to the field of petroleum cracking, in particular to a low-carbon olefin cracking device for cracking crude oil in a reduced pressure environment and a cracking method for preparing low-carbon olefin by adopting the low-carbon olefin cracking device.

Background

The low-carbon olefin is a general term for unsaturated hydrocarbons with four or less carbon atoms, and mainly includes organic chemical raw materials with high economic value, such as ethylene, propylene, isobutene, butadiene and the like. With the economic development of China, the demand of the organic chemical raw materials is increased year by year, and although the production scale of the low-carbon olefin is also increased year by year, the increased demand cannot be met. The technology for effectively improving the yield of the low-carbon olefin has wide application prospect.

For a long time, petroleum hydrocarbon cracking is mainly adopted to prepare low-carbon olefin products. With the large scale of petrochemical enterprise production devices, the processing capacity of a single set of oil refining device is over 1000 ten thousand tons/year, and the ethylene production capacity of a matched ethylene device reaches millions of tons/year. With the development of clean energy, the demand of people for fossil fuels is decreasing, and along with the economic development, the demand of petrochemical products is increasing day by day, and the fuel route of the traditional refinery considering the cracking raw material mode is difficult to meet the requirement.

That is, the heavy hydrocarbons, especially crude oil which is not processed, are used as cracking raw materials, and raw materials of a cracking device are obtained by processing through relatively simplified process units, so that the high investment and operation cost of a plurality of sets of process devices of a traditional large-scale oil refinery can be avoided, the raw material cost and the energy consumption of an olefin production device can be reduced, and the change of market supply and demand can be adapted.

In the cracking apparatus, the core is a tubular cracking furnace (hereinafter referred to as "cracking furnace"), and when a cracking raw material such as petroleum hydrocarbon is heated to a high temperature in the cracking furnace, a chemical reaction of carbon chain breaking occurs to generate target products such as low-carbon olefins such as ethylene, propylene and butadiene.

In order to reduce the construction investment and the production cost, the patentee has carried out the researches of enlarging the cracking furnace, improving and increasing the selectivity and the product yield of the cracking furnace, prolonging the operation period of the cracking furnace and the like. In particular, the size of cracking furnaces has been increasing with the increase in the size of ethylene plants.

Patent CN921048882 describes a pyrolysis furnace in which vertical tubes are arranged in a plurality of parallel rows, each row being heated by a bottom burner parallel to the row, the radiant section being preferably cuboidal, i.e. having a height, a length and a width substantially equal to each other.

Patent CN038135825 describes a pyrolysis furnace with more uniform heating, comprising two convection sections arranged along opposite sides of the radiant section, with the cracking furnace tubes arranged in parallel rows, each row being arranged parallel to each other in the radiant section hearth, with burners arranged between the tube rows.

Patent CN200710118074 proposes an ethylene cracking furnace, in which furnace tubes are located in a radiation section, each furnace tube is composed of an inlet tube and an outlet tube, the furnace tubes are arranged in two rows in the radiation section, each row forms a tube row plane, the inlet tubes and the outlet tubes of the furnace tubes are respectively located in two different tube row planes in an alternate and spaced manner, and are connected together at the bottom through a symmetrical U-shaped connecting piece. The large-scale cracking furnace can be realized, the radiation heat transfer efficiency is improved by the furnace tube arrangement mode, the operation period is prolonged, and the energy consumption of products is reduced.

Patent CN2014102289158 describes a cracking furnace, the bottom of the radiation section of which is provided with four rows of burners and two groups of radiation furnace tubes, each group of radiation furnace tubes is arranged in two rows, so that four rows of radiation furnace tubes are arranged in the radiation section, and the cracking furnace is considered to be large-sized, and occupied land and investment are reduced.

Patent CN2014102292004 describes an ethylene cracking furnace, which comprises a radiation section, a convection section, a quenching heat exchanger, an induced draft fan and a chimney, wherein two rows of radiation furnace tubes are arranged in the radiation section, the radiation furnace tubes comprise an inlet tube row formed by a row of inlet tubes and an outlet tube row formed by a row of outlet tubes, a plurality of burners are arranged on two sides of the two rows of radiation furnace tubes, and the burners are arranged to supply heat to the radiation furnace tubes asymmetrically, so that the heat release of the burners close to the inlet tube row is greater than that of the burners close to the outlet tube row. The cracking furnace is long in operation period, high in product yield and high in production capacity.

Patent CN2013102366997 discloses an ethylene cracking furnace, which comprises a radiation section coil assembly, the assembly is composed of X-type radiation coil modules arranged in the radiation section along the length direction of the furnace body and perpendicular to the bottom surface, each X-type radiation coil module is composed of four groups of radiation coils, and each group of radiation coils is composed of furnace tubes. The four groups of radiation coil pipes are connected with a four-in-one stereo polymerization pipe as a material outlet at the center of the X-type radiation coil pipe module, the farthest gateway of the four groups of radiation coil pipes from the center of the X-type radiation coil pipe module is used as an inlet of the material and is connected with an inlet collecting pipe, and the bottom burner is arranged at the gap between every two adjacent radiation coil pipes. It is believed that each furnace tube on each independent radiant coil of the invention is heated uniformly, prolonging the service life of the furnace tubes and improving the ethylene production capacity.

However, the above patents focus on how to arrange the furnace tubes in the radiant section of the cracking furnace to ensure that more tubes are arranged in the furnace and improve the radiant heat transfer, so that the temperature of the material in the furnace tubes can be raised quickly in a very short residence time. However, in any arrangement, the tube rows are in a certain plane or two vertically-alternating planes, the furnace tubes are still in linear distribution, and the inlet furnace tubes and the outlet furnace tubes are in crossed arrangement. The tube rows of the furnace tubes are arranged in the same plane, for two-pass furnace tubes widely applied to the cracking furnace, inlet tubes and outlet tubes of the two-pass furnace tubes need to be connected, and the two-pass furnace tubes are arranged in the same plane, so that the mutual intersection of each radiation furnace tube (comprising one inlet tube and one outlet tube) is undoubtedly brought, the length or the structure of each radiation furnace tube is inconsistent, the small difference in the structure among the furnace tubes is formed, and the reaction of cracking raw materials in the furnace tubes is further influenced.

In addition, from the standpoint of the heat transfer of the furnace, fuel gas (primarily methane and hydrogen) is combusted to provide heat within the furnace chamber of the furnace, which enters the furnace tubes by both radiant and convective heat transfer. Generally, a cracking furnace uses mixed combustion of fuel gas and air to provide heat for cracking reaction, the combustion reaction is caused by high energy collision between combustible molecules in the fuel and oxygen molecules, so that the supply condition of oxygen determines the combustion process.

The traditional cracking furnace generally adopts air as combustion-supporting gas, because oxygen content in the air is only 21%, most is nitrogen gas, consequently in the combustion process, the burning velocity of fuel gas is slower, and burning flame is longer, and in cracking furnace's direction of height, furnace temperature is the curve and distributes, and is few in furnace bottom heat supply, and furnace middle part is then the heat supply is the most, and furnace upper portion heat supply begins to reduce. For a cracking furnace with a multi-pass furnace tube, because the residence time is long, the contradiction between hearth heat supply and furnace tube heat absorption is not outstanding, but for a single-pass furnace tube, the contradiction is prominent. In a one-way furnace tube, materials are continuously and rapidly heated at the inlet end of the furnace tube, and a large amount of heat is continuously generated, however, the heat supply quantity at the bottom of the traditional combustion system is less; at the outlet end of the furnace tube, the coking rate of the materials is increased sharply, secondary reaction needs to be controlled, and the heat supply at the middle upper part of the traditional combustion system is maximized. That is, there is a matching problem between the combustion system and the once-through furnace tubes.

If oxygen-enriched air with higher oxygen concentration than air is adopted for combustion, compared with the conventional air combustion, the method has the following advantages: firstly, because the radiation heat transfer is the main mode of pyrolysis furnace heat transfer, according to the characteristics of gas radiation, only the triatomic gas and polyatomic gas have the radiation ability, and the diatomic gas has almost no radiation ability, and under the combustion-supporting condition of conventional air, the proportion of nitrogen gas without radiation ability is very high, and the blackness of flue gas is very low, has influenced the radiation heat transfer process of flue gas to the boiler tube bank. Oxygen-enriched air is adopted for combustion supporting, and the nitrogen content is low, so that the air quantity and the flue gas quantity are both obviously reduced, the flame temperature and the blackness are obviously improved along with the increase of the oxygen proportion in the combustion air, the flame radiation intensity is further improved, and the radiation heat transfer is enhanced; secondly, oxygen-enriched air is adopted for supporting combustion, the flame of combustion is shortened, the combustion intensity is improved, the combustion speed is accelerated, the complete combustion reaction is facilitated, the use efficiency of fuel is improved, and the thermal efficiency of the cracking furnace is further improved; and thirdly, oxygen-enriched air is adopted for combustion supporting, so that the excess air coefficient can be properly reduced, the smoke exhaust volume is reduced, the smoke quantity after combustion is reduced, the smoke exhaust loss is further reduced, and the energy conservation of the cracking furnace is promoted.

From the view point of the furnace chamber of the cracking furnace, the heat required by the reaction of the furnace tube of the cracking furnace is provided by the furnace chamber, fuel gas (mainly methane and hydrogen) is combusted to provide heat in the furnace chamber of the cracking furnace, and the heat enters the furnace tube through radiation heat transfer and convection heat transfer, wherein the radiation heat transfer is the main heat transfer mode and accounts for more than 85 percent of the total heat transfer. The radiation heat transfer of the hearth of the cracking furnace is influenced by various complex factors, such as the structure and the size of the hearth, the type and the heat supply mode of fuel, the type of a burner and the like. At present, the traditional cracking furnace adopts ceramic fiber or refractory bricks as the furnace wall of the cracking furnace, the reaction materials in the radiation furnace tube of the cracking furnace are heated by utilizing the high-temperature flue gas combusted by fuel gas and the radiation heat transfer of the furnace wall, the furnace wall of the cracking furnace adopts a flat furnace wall structure, and the radiation of the furnace wall of the cracking furnace is the same for the inlet part and the outlet part of the furnace tube from the radiation heat transfer angle.

The heat transfer process of the hearth of the cracking furnace at present has the following two problems that firstly, the heat transfer area of the hearth of the cracking furnace is insufficient, the heat transfer process of the hearth of the cracking furnace mainly adopts radiation heat transfer, and the radiation heat transfer quantity mainly depends on the heat transfer area of a radiation surface. For the furnace tubes, the external surface area is basically determined when the capacity of the cracking furnace is determined, and the cost is high due to the high price of the furnace tubes. For the furnace wall, the surface area is related to the size of the hearth and the shape of the furnace wall. Secondly, the radiant heat transfer of the furnace wall of the cracking furnace has no difference for the furnace tube rows, namely the furnace wall of the cracking furnace has consistent heat transfer area for the inlet tube row or the outlet tube row, and is also the same for a region with large heat flux and a region with small heat flux, which can cause the local heating of the cracking furnace to be uneven, thereby causing the local temperature of the furnace tube to be overhigh and reducing the operation period of the cracking furnace.

Patent EP0059772 provides a method for preparing low carbon olefins by cracking residual crude oil with crude oil in an adiabatic reactor by using heat generated by combustion of a portion of crude oil, which can directly use unprocessed crude oil to obtain low carbon olefins, but due to the adoption of the adiabatic reactor design, only an intermittent process can be used, which greatly reduces the production efficiency, and the process requires combustion of a portion of crude oil as fuel, thereby greatly reducing the yield of low carbon olefins, and is not an economical and effective method for preparing low carbon olefins.

The patents US3617493 and CN1957068 use the existing process flow of preparing low-carbon olefin from petroleum hydrocarbon, and a flash separator is arranged in the convection section of the cracking furnace to separate the components which cannot be fully gasified from the petroleum hydrocarbon, and the obtained light components are sent to the radiation section of the cracking furnace for cracking reaction to obtain the low-carbon olefin. The scheme effectively solves the problem of continuous production of low-carbon olefins, but the crude oil needs to be cut, part of the crude oil cannot be fully utilized, and the problem of utilization efficiency of the crude oil cannot be solved.

Patent WO2008091439/CN101583697 proposes to mix crude oil into the existing ethylene production raw material, dilute the crude oil, improve the cracking performance of the crude oil, and improve the operability of a cracking furnace, thereby increasing the conversion rate of olefins, but is limited by the source of the existing ethylene production raw material, and cannot effectively utilize a large amount of crude oil to produce low-carbon olefins.

Patents such as WO2013142605/US2013033156, US20130233766, US20130248417, WO2013142609/US2013033165, WO2013142617/US2013033181, US20130228495 and the like propose that the existing steam cracking process is combined with a slurry type hydrogenation process, a hydrocracking process, a catalytic cracking process, a delayed coking process and the like, and other processes are utilized to improve the BMCI value of the crude oil, so that the crude oil obtains better cracking performance, the coking of a cracking furnace is effectively reduced, and heavy part materials in the crude oil are fully utilized, so that the benefit of the whole process is improved. But the processing process of crude oil in the earlier stage of the technology is complex, the production cost of the low-carbon olefin is increased, and the low-carbon olefin produced by the technology hardly has good market competitiveness.

Therefore, there is a need to solve the problems of crude oil not being directly used as cracking feedstock and high cost of producing light olefins.

Disclosure of Invention

The invention aims to overcome the problem that the crude oil cannot be directly used as cracking raw material in the prior art.

The inventor of the application creatively discovers through a great deal of research that the crude oil can be rapidly gasified in a negative pressure environment, so that the crude oil can be directly used as a cracking raw material without complex treatment, and finally, the low-carbon olefin can be produced at lower cost than the prior art.

In order to achieve the above object, in one aspect, the present invention provides a low carbon olefin cracking apparatus, which includes a convection section, a radiation section, a quenching boiler, a separation tower, and a pressure reduction device, which are sequentially connected to each other, wherein the pressure reduction device keeps a material flowing through a material pipeline of the convection section, the radiation section, the quenching boiler, and the separation tower in a negative pressure state, and the radiation section includes a furnace chamber, a furnace wall disposed on an inner wall of the furnace chamber, at least one tube bundle disposed inside the furnace chamber, and a plurality of burners disposed on a side wall and/or a bottom wall of the furnace chamber.

Preferably, the burner is fuelled with methane or a methane-hydrogen mixture and oxygen-enriched air as the combustion-supporting gas.

Preferably, the concentration of the oxygen-enriched air is 25-40%; more preferably, the oxygen-enriched air has a concentration of 27-33%.

Preferably, the heat supply proportion of the burner arranged on the bottom wall of the hearth is 60-100%; more preferably, the heat supply proportion of the burner arranged on the bottom wall of the hearth is 70-100%.

Preferably, the tube bundle comprises a plurality of furnace tubes arranged in a circle or an ellipse centered on a center point of the tube bundle.

Preferably, the tube bundle comprises 4-20 of the furnace tubes; more preferably, the tube bundle comprises 6 to 12 of the furnace tubes.

Preferably, the distance between the furnace tube and the center of the tube bundle is 350-1500 mm; more preferably, the distance between the furnace tube and the center of the tube bundle is 400-1200 mm.

Preferably, the furnace tubes are single pass furnace tubes or multiple pass furnace tubes.

Preferably, when the furnace tube is a single-pass furnace tube, the single-pass furnace tube is a tube with a constant tube diameter or a tube with a gradually increased tube diameter from the inlet end to the outlet end.

Preferably, when the one-way furnace tube is a tube with a gradually increased tube diameter from the inlet end to the outlet end, the inner diameter of the tube opening of the inlet end is 25-60 mm; more preferably, the inner diameter of the pipe orifice of the inlet end is 35-45 mm.

Preferably, when the one-way furnace tube is a tube with a gradually increased tube diameter from the inlet end to the outlet end, the inner diameter of a tube opening of the outlet end is 35-75 mm; preferably, the inner diameter of the pipe orifice of the outlet end is 45-65 mm.

Preferably, the ratio of the distance between the single-pass furnace tubes to the diameter of the single-pass furnace tubes is 1.2-3.0; more preferably, the ratio of the distance between the furnace tubes to the diameter of the furnace tubes is 1.6-2.2.

Preferably, when the furnace tube is a multi-pass furnace tube, the multi-pass furnace tube is a two-pass furnace tube, a four-pass furnace tube or a six-pass furnace tube; more preferably, the multi-pass furnace tube is a two-pass furnace tube.

Preferably, the multi-pass furnace tube comprises a plurality of radiant furnace tubes, each radiant furnace tube comprising one or more inlet tubes, one outlet tube, and a connecting tube connecting the inlet tubes and the outlet tubes.

Preferably, the ratio of the inner diameter of the outlet pipe to the inner diameter of the inlet pipe is greater than 1 and 2.5 or less.

Preferably, the inner diameter of the inlet pipe is 25-60 mm; more preferably, the inner diameter of the inlet pipe is 35 to 55 mm.

Preferably, the inner diameter of the outlet pipe is 45-140 mm; more preferably, the inner diameter of the outlet pipe is 55-95 mm.

Preferably, the ratio of the distance between the multi-pass furnace tubes to the diameter of the multi-pass furnace tubes is 1.2-5.0; more preferably, the ratio of the distance between the multi-pass furnace tubes to the diameter of the multi-pass furnace tubes is 1.6-3.0.

Preferably, an enhanced heat transfer element is arranged in the furnace tube.

Preferably, the lower olefin cracking apparatus further comprises a reboiler disposed at the bottom of the separation column and a condenser disposed between the separation column and the pressure reducing device.

In another aspect of the present invention, a cracking method is provided, where the method is implemented by using the low carbon olefin cracking apparatus provided in the present invention, and the method includes: the method comprises the following steps: the materials enter a convection section for gasification, and the gasified materials enter a radiation section for cracking; step two: the pyrolysis product obtained in the first step enters a quenching boiler for primary cooling; step three: and (3) the cracking product after the primary cooling in the second step enters a separation tower to be separated so as to obtain tar and cracking gas, wherein the gasification and the cracking are carried out under the negative pressure condition through a pressure reducing device.

Preferably, the method further comprises: step four: and separating the pyrolysis gas in a separation unit to obtain the low-carbon olefin.

Preferably, the negative pressure is 0.5-101 KPa; more preferably, the negative pressure is 1-10 KPa.

Preferably, the residence time of the materials in the radiation section is 50-500 ms; more preferably, the residence time of the material in the radiation section is 100-400 ms.

The invention uses the pressure reducing device to make the pipelines of the convection section, the radiation section and the quenching boiler flowing through the materials in the negative pressure state, therefore, when the heavy cracking raw material (such as crude oil) enters the convection section, the gasification temperature is reduced under the negative pressure condition, thereby the heavy cracking raw material can be quickly and fully gasified.

Drawings

FIG. 1 is a schematic view of the structure of a cracking apparatus used in one embodiment of the present invention.

FIG. 2 is a schematic top view of a conventional furnace tube arrangement cracking furnace.

FIG. 3 is a schematic top view of a 1-1 type two-pass furnace tube according to the present invention.

FIG. 4 is a schematic top view of a 2-1 type two-pass furnace tube according to the present invention.

FIG. 5 is a schematic top view of a single pass furnace tube cracking furnace of the present invention.

FIG. 6 is a schematic top view of a pyrolysis furnace of the present invention with two tube bundles arranged in a row.

FIG. 7 is a schematic top view of a pyrolysis furnace of the present invention with three tube bundles arranged in rows.

FIG. 8 is a schematic top view of a four tube bundle cracking furnace of the present invention.

FIG. 9 is a schematic top view of an oval tube bundle cracking furnace of the present invention.

Description of the reference numerals

1 fan 2 convection section

3 tube bundle 4 burner

5 radiation section 6 quenching boiler

7 reboiler 8 separation column

9 condenser 10 pressure reducing device

11 furnace wall 12 furnace tube

Detailed Description

The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

Hereinafter, referring to fig. 1 to 9, the low carbon olefin cracking apparatus and the cracking method provided by the present invention will be described in detail.

Referring to fig. 1, the low-carbon olefin cracking apparatus provided by the present invention includes a fan 1, a convection section 2, a radiation section 5, a quenching boiler 6, a separation tower 8, a condenser 9, and a pressure reduction device 10. Cracking raw materials enter a convection section 2 under the action of a fan 1, after the convection section 2 is gasified, cracking is carried out in a radiation section 5, then a cracking product enters a quenching boiler 6 for primary cooling, then enters a separation tower 8 for separation, and is separated into tar and cracking gas, the tar enters the next unit (further processed or packaged into a product), the cracking gas is separated through a separation unit (for example, a conventional ethylene device), and finally a low-carbon olefin product is obtained. In the present invention, the pressure reducing device 10 is added to the cracking apparatus, and the pipelines through which the materials flow in the convection section 2, the radiation section 5, the quenching boiler 6 and the separation tower 8 can be all in a negative pressure state by the pressure reducing device 10.

Through the pressure reducer, all be in the negative pressure state with the pipeline of the material that flows through of convection section, the radiation section, quench boiler and knockout tower, when heavy pyrolysis raw materials (such as crude oil) got into the convection section, its gasification temperature reduces under the negative pressure condition, thereby can gasify fast and fully, compare with traditional ordinary pressure technology, need not to carry out the preliminary treatment with heavy pyrolysis raw materials, direct use also can fully gasify at the convection section as pyrolysis raw materials, consequently, can save the technology cost, simultaneously, because gasify under the lower temperature of relative ordinary pressure, thereby can not reach the coking temperature, effectively reduce the coking of pyrolysis furnace.

In the present invention, except for the radiation section, other devices may be adopted by products conventional in the art, and the present invention is not specifically described. Therefore, the following will be described in detail with respect to the radiation section.

As shown in fig. 1, 3 to 9, the radiant section 5 comprises a furnace, a furnace wall 11 arranged on the inner wall of the furnace, at least one tube bundle 3 arranged inside the furnace and a plurality of burners 4 arranged on the side and/or bottom wall of the furnace. The tube bundle, the furnace wall, and the burner are explained in detail in this order.

In the present invention, the tube bundle 3 includes a plurality of furnace tubes 12 arranged in a circular shape (see fig. 3 to 8) or an elliptical shape (see fig. 9) centering on the center of the tube bundle, and preferably, the plurality of furnace tubes 12 are uniformly distributed. One tube bundle (as shown in fig. 3 to 5) or two, three or four tube bundles (as shown in fig. 6 and 8) may be disposed in the furnace chamber of the cracking furnace, and each tube bundle has the same structure (structure and number of furnace tubes), but the invention is not limited thereto. In the present invention, the tube bundle 3 may include 4 to 20 furnace tubes 12, and more preferably, the tube bundle 3 includes 6 to 12 furnace tubes 12. In addition, the distance between the furnace tube and the center of the tube bundle is 350-1500 mm, and more preferably 400-1200 mm.

The conventional furnace tubes are linearly distributed (as shown in fig. 2), so that the furnace tubes have the problems of large floor space, different heating among the furnace tubes and the like. However, with the arrangement of the furnace tubes provided by the invention, the furnace tubes are uniformly distributed in the hearth in a circular or elliptical shape, so that the differences of heating and the like among the furnace tubes are reduced, and the production capacity of the cracking furnace per unit floor area is greatly improved (in other words, the floor area of the cracking furnace is reduced under the condition of the same feeding amount).

In the invention, the furnace tube can be a single-pass furnace tube or a multi-pass furnace tube.

When the furnace tube is a one-way furnace tube, the one-way furnace tube is a tube with constant tube diameter or a tube with gradually increased tube diameter from the inlet end to the outlet end. When the one-way furnace tube is a tube with the tube diameter gradually increased from the inlet end to the outlet end, the inner diameter of the tube opening of the inlet end is preferably 25-60 mm, and more preferably 35-45 mm; the inner diameter of the pipe orifice of the outlet end is preferably 35-75 mm, and more preferably 45-65 mm. In addition, the ratio of the distance between the single-pass furnace tubes to the diameter of the single-pass furnace tubes is 1.2 to 3.0, and more preferably 1.6 to 2.2.

When the furnace tube is a multi-pass furnace tube, the multi-pass furnace tube is a two-pass furnace tube, a four-pass furnace tube or a six-pass furnace tube, and more preferably the multi-pass furnace tube is a two-pass furnace tube. The multi-pass furnace tube comprises a plurality of radiant furnace tubes, each preferably formed to include one or more inlet tubes, one outlet tube, and connecting tubes connecting the inlet and outlet tubes. Of course, each radiant furnace tube may also be in a shape with a gradually increasing tube diameter under the condition allowed by the manufacturing process. On this basis, the ratio of the inner diameter of the outlet pipe to the inner diameter of the inlet pipe is preferably greater than 1 and 2.5 or less. In addition, the inner diameter of the inlet pipe is 25-60 mm, and more preferably 35-55 mm; the inner diameter of the outlet pipe is 45-140 mm, and more preferably 55-95 mm. In addition, the ratio of the distance between the multipass furnace tubes to the diameter of the multipass furnace tubes is 1.2-5.0, more preferably 1.6-3.0, and specifically, the ratio refers to the ratio of the distance between the inlet tubes in the multipass furnace tubes to the diameter of the inlet tubes and the ratio of the distance between the outlet tubes in the multipass furnace tubes to the diameter of the outlet tubes.

In addition, in order to improve the heat transfer efficiency in the furnace tube, a heat transfer enhancing element can be arranged in the furnace tube. The heat transfer enhancing elements may be spiral sheet inserts, twisted ribbon inserts, cross zigzag inserts, coil core inserts, filament wound porous bodies, spherical matrix inserts, etc., or different heat transfer enhancing element combinations may be provided in different portions of the furnace tube, and the present invention is not particularly limited with respect to the heat transfer enhancing elements and their arrangement.

In addition, in the present invention, the burners 4 may be disposed on the bottom wall and/or the side wall of the furnace, wherein, preferably, the heat supply ratio of the burners disposed on the bottom wall of the furnace is 60 to 100%, more preferably 70 to 100%, where, the heat supply ratio of the burners on the bottom wall means that the heat supply of the burners on the bottom wall accounts for the sum of the heat supply of the burners on the side wall of the furnace and the burners on the bottom wall of the furnace, for example, when the heat supply ratio of the burners on the bottom wall is 100%, the burners are disposed only on the bottom wall of the whole furnace, and no burners are disposed on the side wall. In addition, the combustor 4 uses methane or a methane-hydrogen mixture as fuel and oxygen-enriched air as combustion-supporting gas, wherein the concentration of the oxygen-enriched air is preferably 25-40%, and more preferably 27-33%.

The invention adopts the oxygen-enriched air with higher oxygen concentration than air to burn, and has more advantages compared with air burning: firstly, because radiation heat exchange is a main heat transfer mode of a cracking furnace, only three-atom gas and multi-atom gas have radiation capacity according to the characteristics of gas radiation, diatomic gas almost has no radiation capacity, under the condition of conventional air combustion supporting, the proportion of nitrogen without radiation capacity is very high, the blackness of flue gas is very low, the radiation heat transfer process of the flue gas to a furnace tube bank is influenced, oxygen-enriched air is adopted for combustion supporting, and because the content of nitrogen is low, the air quantity and the flue gas quantity are both remarkably reduced, the flame temperature and the blackness are remarkably improved along with the increase of the proportion of oxygen in combustion air, so that the flame radiation intensity is improved, and the radiation heat transfer is enhanced; secondly, oxygen-enriched air is adopted for supporting combustion, the flame of combustion is shortened, the combustion intensity is improved, the combustion speed is accelerated, the complete combustion reaction is facilitated, the use efficiency of fuel is improved, and the thermal efficiency of the cracking furnace is further improved; and thirdly, oxygen-enriched air is adopted for combustion supporting, so that the excess air coefficient can be properly reduced, the smoke exhaust volume is reduced, the smoke quantity after combustion is reduced, the smoke exhaust loss is further reduced, and the energy conservation of the cracking furnace is promoted.

In addition, the low carbon olefin cracking apparatus of the present invention further comprises a reboiler 7 disposed at the bottom of the separation column 8 and a condenser 9 disposed between the separation column 8 and the pressure reducing device 10. The reboiler 7 vaporizes the gaseous material in the cracked product sufficiently to carry away the liquid material, and the condenser is used to further remove the liquid component from the gaseous product (cracked gas) flowing out of the separation column 8. In general, both the reboiler and the condenser are used to assist the separation column in achieving adequate separation of the gases and liquids in the cracked product.

In summary, the light olefin cracking apparatus according to the preferred embodiment of the present invention has the following advantages:

1) the pipelines of the convection section, the radiation section and the quenching boiler through which the materials flow are all in a negative pressure state through the pressure reducing device, so that heavy petroleum hydrocarbons such as crude oil can be directly used as cracking raw materials, the process cost can be saved, and the coking of the cracking furnace can be effectively reduced;

2) the furnace tubes are uniformly distributed in the hearth in a circular or oval shape, so that the differences of heating and the like among the furnace tubes are reduced, and the production capacity of the cracking furnace in unit floor area is greatly improved;

3) the oxygen amount carried in the oxygen-enriched air adopted by the burner is increased, the nitrogen amount is reduced, the gas can be saved, and simultaneously, the yield of the low-carbon olefin is improved due to the relative increase of the reaction heat.

The low-carbon olefin cracking equipment provided by the invention is explained in detail above. Next, the present invention provides a cracking method.

The cracking method provided by the invention is realized by adopting the low-carbon olefin cracking equipment provided by the invention, and the method comprises the following steps: the method comprises the following steps: the materials enter the convection section 2 to be gasified, and the gasified materials enter the radiation section 5 to be cracked; step two: cooling the cracked product obtained in the first step in a quenching boiler 6 to obtain a liquid product; step three: and (3) enabling the liquid product obtained in the step (II) to enter a separation tower 8 for separation so as to obtain tar and pyrolysis gas, and performing the step (IV): and (3) separating the pyrolysis gas in a separation unit to obtain the low-carbon olefin, wherein the gasification and the pyrolysis are carried out under a negative pressure condition through a pressure reducing device 10, preferably, the negative pressure is controlled to be 0.5-101 KPa, and more preferably, the negative pressure is controlled to be 1-10 KPa. In addition, the retention time of the materials in the radiation section 5 is 50-500 ms, and more preferably 100-400 ms.

The present invention will be described in detail below by way of examples.

Example 1

The cracking reaction is carried out by adopting the low-carbon olefin cracking equipment (shown in figure 1). The low-carbon olefin cracking equipment comprises a fan 1, a convection section 2, a radiation section 5, a quenching boiler 6, a reboiler 7, a separation tower 8, a condenser 9 and a pressure reduction device 10.

Firstly, starting the pressure reducing device 10, and controlling the pressure of the equipment to be 5KPa, so that the equipment is in a negative pressure state; the removed crude oil is gasified and preheated through a convection section 2 and then enters a radiant section furnace tube 3 for cracking reaction; the combustion system of the radiation section 5 adopts a combination mode of a bottom combustor and a side wall combustor, the heat supply proportion of the bottom combustor is 80%, the combustor adopts oxygen-enriched air for combustion, and the oxygen concentration in the oxygen-enriched air is 30% (V/V). The preheating temperature of the stripped crude oil in the convection section, namely the crossing temperature (XOT) of the cracking furnace is 550 ℃, the outlet temperature (COT) of the radiation section of the cracking furnace is 800 ℃, the furnace tube of the radiation section adopts a 1-1 type furnace tube, the diameter of the inlet tube of the furnace tube is 56mm, the diameter of the outlet tube of the furnace tube is 64mm, the length of the furnace tube is 26.4m, and the furnace tube adopts an upward-going and upward-going mode. The furnace tubes are arranged in a novel manner as shown in fig. 7. The properties of the cracking feedstock (crude oil after stripping) are shown in Table 1, the process parameters of the cracking furnace are shown in Table 2, and the composition of the fuel gas of the cracking furnace is shown in Table 3.

Comparative example 1

And (3) carrying out cracking reaction by adopting a conventional cracking device. The specific process comprises the following steps:

under the normal pressure state, the removed crude oil (properties are shown in table 1) is gasified and preheated in a convection section, and then enters a radiant section furnace tube for cracking reaction, a combustion system of the radiant section adopts a mode of combining a bottom combustor and a side wall combustor, the heat supply proportion of the bottom combustor is 80%, and the combustor adopts air for combustion; the preheating temperature of the stripped crude oil in the convection section, namely the crossing temperature (XOT) of the cracking furnace is 550 ℃, the outlet temperature (COT) of the radiation section of the cracking furnace is 800 ℃, the furnace tube of the radiation section adopts a 1-1 type furnace tube, the diameter of the inlet tube of the furnace tube is 56mm, the diameter of the outlet tube of the furnace tube is 64mm, the length of the furnace tube is 26.4m, and the furnace tube adopts an upward-going and upward-going mode. The furnace tubes are arranged in a conventional manner as shown in FIG. 2. The process parameters of the cracking furnace are shown in Table 2, and the composition of the fuel gas of the cracking furnace is shown in Table 3.

TABLE 1 crude oil Properties after stripping

TABLE 2

TABLE 3 Fuel gas composition

Components	mol％
		Hydrogen gas	3.6
Methane	95.8
		Ethane (III)	0.23
Propane	0.08
		Others	0.29
Total up to	100.00

From the results of example 1 and comparative example 1, it can be seen that the low carbon olefin cracking apparatus of the present invention has the following advantages compared with the conventional cracking apparatus:

1) when the crude oil is put into use, the operation period of the comparative example 1 can only be maintained for 5 days, while the operation period of the cracking equipment can be maintained for 43 days in the example 1, and the operation period of the cracking equipment is greatly prolonged under a negative pressure environment, so that the low-carbon olefin cracking device can ensure the normal use of the crude oil in the cracking equipment, and the process cost can be saved;

2) the same charge was used in example 1 as in comparative example 1, but the floor space of the furnace was 72m from that of comparative example 1²Reduced to 28m of example 1²Under the same process conditions, compared with the comparative example 1, in the example 1, because the operation conditions of all groups of furnace tubes are uniform, the differences of heating and the like among the furnace tubes are reduced, and the production capacity of the cracking furnace in unit floor area is greatly improved;

3) the nitrogen amount carried by the combustion-supporting oxygen after the oxygen-enriched combustion is adopted is reduced, the yield of the low-carbon olefin is effectively improved (the reaction heat is increased), and simultaneously, the fuel consumption is compared with that of a comparative example 1(8100 Nm/Nm)³Instead,/h) is reduced (8010 Nm)³/h)。

The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.

Claims

1. The low-carbon olefin cracking equipment is characterized by comprising a convection section (2), a radiation section (5), a quenching boiler (6), a separation tower (8) and a pressure reducing device (10) which are sequentially communicated, wherein the pressure reducing device enables pipelines of materials flowing through the convection section (2), the radiation section (5), the quenching boiler (6) and the separation tower (8) to be in a negative pressure state, and the radiation section (5) comprises a hearth, a furnace wall (11) arranged on the inner wall of the hearth, at least one tube bundle (3) arranged inside the hearth and a plurality of burners (4) arranged on the side wall and/or the bottom wall of the hearth.

2. The low carbon olefin cracking apparatus according to claim 1, wherein the combustor (4) uses methane or a methane-hydrogen mixture as fuel and oxygen-enriched air as combustion-supporting gas.

3. The low-carbon olefin cracking equipment of claim 2, wherein the concentration of the oxygen-enriched air is 25-40%.

4. The lower olefin cracking apparatus of claim 3, wherein the oxygen-enriched air has a concentration of 27-33%.

5. The low-carbon olefin cracking equipment of claim 1, wherein the heat supply ratio of the burner arranged on the bottom wall of the hearth is 60-100%.

6. The low-carbon olefin cracking equipment of claim 5, wherein the heat supply proportion of the burner arranged on the bottom wall of the hearth is 70-100%.

7. The lower olefin cracking apparatus of claim 1, wherein the tube bundle (3) comprises a plurality of tubes (12) arranged in a circular or elliptical shape centered on a center point of the tube bundle.

8. The low carbon olefin cracking apparatus of claim 7, wherein the tube bundle (3) comprises 4-20 of the furnace tubes (12).

9. The low carbon olefin cracking apparatus of claim 8, wherein the tube bundle (3) comprises 6 to 12 tubes (12).

10. The low carbon olefin cracking apparatus of claim 7, wherein the distance between the furnace tube and the center of the tube bundle is 350-1500 mm.

11. The low carbon olefin cracking apparatus of claim 10, wherein the distance between the furnace tube and the center of the tube bundle is 400-1200 mm.

12. The low carbon olefin cracking apparatus of claim 7, wherein the furnace tubes are single pass furnace tubes or multi-pass furnace tubes.

13. The low carbon olefin cracking apparatus of claim 12, wherein when the furnace tubes are single pass furnace tubes, the single pass furnace tubes are tubes with a constant tube diameter or tubes with a gradually increasing tube diameter from an inlet end to an outlet end.

14. The low carbon olefin cracking apparatus of claim 13, wherein when the once-through furnace tubes are tubes with gradually increasing tube diameters from the inlet end to the outlet end,

the inner diameter of the pipe orifice of the inlet end is 25-60 mm.

15. The low carbon olefin cracking apparatus of claim 14, wherein when the once-through furnace tubes are tubes with gradually increasing tube diameters from the inlet end to the outlet end,

the inner diameter of the pipe orifice of the inlet end is 35-45 mm.

16. The low carbon olefin cracking apparatus of claim 13, wherein when the once-through furnace tubes are tubes with gradually increasing tube diameters from the inlet end to the outlet end,

the inner diameter of the pipe orifice of the outlet end is 35-75 mm.

17. The low carbon olefin cracking apparatus of claim 16, wherein when the once-through furnace tubes are tubes with gradually increasing tube diameters from the inlet end to the outlet end,

the inner diameter of the pipe orifice of the outlet end is 45-65 mm.

18. The low carbon olefin cracking apparatus of claim 13, wherein the ratio of the spacing between the single pass furnace tubes to the diameter of the single pass furnace tubes is 1.2-3.0.

19. The low carbon olefin cracking apparatus of claim 13, wherein the ratio of the spacing between the single pass furnace tubes to the diameter of the single pass furnace tubes is 1.6-2.2.

20. The apparatus of claim 12, wherein when the furnace tube is a multi-pass furnace tube, the multi-pass furnace tube is a two-pass furnace tube, a four-pass furnace tube, or a six-pass furnace tube.

21. The apparatus of claim 20, wherein when the furnace tube is a multi-pass furnace tube, the multi-pass furnace tube is a two-pass furnace tube.

22. The low carbon olefin cracking apparatus of claim 20, wherein the multi-pass furnace tubes comprise a plurality of radiant furnace tubes, each radiant furnace tube comprising one or more inlet tubes, one outlet tube, and connecting tubes connecting the inlet tubes and the outlet tubes.

23. The lower olefin cracking apparatus of claim 22, wherein the ratio of the inner diameter of the outlet pipe to the inner diameter of the inlet pipe is greater than 1 and 2.5 or less.

24. The low carbon olefin cracking apparatus of claim 22, wherein the inlet pipe has an inner diameter of 25-60 mm.

25. The low carbon olefin cracking apparatus of claim 24, wherein the inlet pipe has an inner diameter of 35-55 mm.

26. The low carbon olefin cracking apparatus of claim 22, wherein the outlet pipe has an inner diameter of 45-140 mm.

27. The low carbon olefin cracking apparatus of claim 26, wherein the outlet pipe has an inner diameter of 55-95 mm.

28. The low carbon olefin cracking apparatus of claim 22, wherein the ratio of the spacing between the multi-pass tubes to the diameter of the multi-pass tubes is 1.2-5.0.

29. The low carbon olefin cracking apparatus of claim 28, wherein the ratio of the spacing between the multi-pass tubes to the diameter of the multi-pass tubes is 1.6-3.0.

30. The low carbon olefin cracking apparatus of claim 7, wherein the enhanced heat transfer element is disposed within the furnace tube.

31. The lower olefin cracking apparatus according to claim 1, further comprising a reboiler (7) disposed at the bottom of the separation column (8) and a condenser (9) disposed between the separation column (8) and the pressure reduction device (10).

32. A cracking method, characterized in that the method is implemented by using the low carbon olefin cracking equipment according to any one of claims 1 to 31, and the method comprises the following steps:

the method comprises the following steps: the materials enter the convection section (2) for gasification, and the gasified materials enter the radiation section (5) for cracking;

step two: the pyrolysis product obtained in the first step enters a quenching boiler (6) for primary cooling;

step three: the cracking product after the primary cooling in the second step enters a separation tower (8) for separation to obtain tar and cracking gas,

wherein the gasification and the pyrolysis are carried out under a negative pressure condition by a pressure reducing device (10).

33. The lysis method according to claim 32, further comprising:

step four: and separating the pyrolysis gas in a separation unit to obtain the low-carbon olefin.

34. The method of cracking claim 32, wherein the negative pressure is 0.5 to 101 Kpa.

35. The cracking process of claim 34, wherein the negative pressure is 1-10 KPa.

36. A cracking process according to claim 32, characterized in that the residence time of the material in the radiant section (5) is 50-500 ms.

37. Cracking process according to claim 36, characterized in that the residence time of the material in the radiant section (5) is 100-400 ms.