CN111233613A - Hydrogenation device and hydrogenation method for producing ethylene and propylene - Google Patents
Hydrogenation device and hydrogenation method for producing ethylene and propylene Download PDFInfo
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- CN111233613A CN111233613A CN202010249488.7A CN202010249488A CN111233613A CN 111233613 A CN111233613 A CN 111233613A CN 202010249488 A CN202010249488 A CN 202010249488A CN 111233613 A CN111233613 A CN 111233613A
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
- C07C7/167—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation for removal of compounds containing a triple carbon-to-carbon bond
Abstract
The invention discloses a hydrogenation device and a hydrogenation method for producing ethylene and propylene, which belong to the field of chemical product production, and comprise a C4 hydrogenation device and a C5 hydrogenation device, wherein C4 and C5 raw materials pass through a raw material buffer tank, a raw material preheater, a static mixer, a hydrogenation reactor, a hydrogenation cooler, a product buffer tank and other equipment, so that dialkenes, alkynes and hydrogen in the C4 and C5 raw materials react to generate mono-olefins under the action of a catalyst, the phenomenon that the dialkenes and alkynes in the C5 raw materials are polymerized to block a pore channel of the catalyst in a downstream OCC reactor is avoided, the coke generation amount is reduced, the switching period of the reactor is prolonged, the diene yield of the OCC device is further improved, and the economic benefit of the device is improved.
Description
Technical Field
The invention relates to the field of chemical product production, in particular to a hydrogenation device and a hydrogenation method for producing ethylene and propylene.
Background
With the large-scale application of Methanol To Olefin (MTO) technology in recent years in China, it is urgent to effectively increase the yield of the target product (ethylene/propylene) and reduce the yield of the MTO technology by-products (C4 and C5: organic substances with 4 carbons and 5 carbons in the MTO by-product). The China Shanghai petrochemical research institute utilizes a ZSM-5 catalyst with unique shape selectivity and acidity to develop a complete set of process for preparing propylene and ethylene by catalytic cracking of C4/C5 olefin, and realizes important technical breakthrough in the field. Practice proves that the OCC technology is used as a 'gold partner' of the MTO technology, has complementary advantages, is used for increasing the yields of propylene and ethylene by cracking C4 and C5 olefins, and greatly improves the overall technical economy of the MTO device.
The OCC technology is a process for preparing propylene and ethylene by further catalytically cracking monoolefins in byproduct C4 and C5 of an MTO device, and then compressing and separating the monoolefins, wherein the higher the content of the monoolefins in C4 and C5 in raw materials of the OCC is, the more beneficial the improvement of the generation of diene (ethylene and propylene) is, the higher the content of the monoolefins in the raw materials of the OCC is, the advantage is that the flow is simple, the operation is convenient, and the energy consumption is lower. The method has the disadvantages that in the actual production process, a certain amount of diene and alkyne components are inevitably contained in the raw materials C4 and C5, and the components are easy to polymerize and block the pore channels of the catalyst in the downstream OCC reactor under a certain condition, so that coke is generated, the switching period of the reactor is reduced, and the yield of the target products (ethylene and propylene) is reduced. Therefore, how to reduce the content of dialkene and alkyne in the raw material C4/C5 of the OCC device and maximally improve the content of single olefin in C4/C5 becomes a problem to be solved urgently for technical improvement of OCC.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a hydrogenation device and a hydrogenation method for producing ethylene and propylene, which can effectively reduce the contents of dialkenes and alkynes in C4 and C5 raw materials in an OCC device, improve the contents of monoolefins in C4 and C5 raw materials and further improve the yield of the dialkenes.
In order to solve the problems, the invention provides the following technical scheme: a hydrogenation unit for producing ethylene and propylene comprises a C4 hydrogenation unit and a C5 hydrogenation unit respectively;
the C4 hydrogenation device comprises a C4 raw material and a hydrogen raw material, wherein the C4 raw material and the hydrogen raw material are supplied outside the device, and the C4 hydrogen raw material is respectively communicated with a first-stage hydrogenation reactor and a second-stage hydrogenation reactor through a C4 hydrogenation pipeline;
the C4 raw material is communicated with the feed end of a C4 raw material buffer tank through a pipeline, the feed end of a C4 raw material buffer tank is provided with a liquid level regulating valve for controlling the liquid level of the C4 raw material, the discharge end of the C4 raw material buffer tank is communicated with a C4 raw material feed pump through a pipeline, the discharge end of a C4 raw material feed pump is communicated with the feed end of a C4 static mixer I through a C4 condensation dehydrator, a C4 filter and a C4 raw material preheater which are sequentially communicated, the discharge end of the C4 raw material feed pump is provided with a flow control valve, and the discharge end of the C4 static mixer I is communicated with the bottom feed inlet of a section of a hydrogenation reactor;
the C4 hydrogenation pipeline comprises a first section of hydrogenation main pipeline, a first section of hydrogenation auxiliary pipeline, a second section of hydrogenation main pipeline and a second section of hydrogenation auxiliary pipeline which are arranged in parallel and provided with valves, the discharge end of the first section of hydrogenation main pipeline is communicated with the feed end of the C4 static mixer I, the discharge end of the first section of hydrogenation auxiliary pipeline is communicated with the middle feed inlet of the first section of hydrogenation reactor, and the top discharge port of the first section of hydrogenation reactor is communicated with a first section of hydrogenation cooler through a pipeline;
a valve is arranged at the feeding end of the first-stage hydrogenation cooler, the discharging end of the first-stage hydrogenation cooler and the discharging end of the second-stage hydrogenation main pipeline are communicated with a C4 static mixer II through pipelines, the discharging end of the C4 static mixer II is communicated with a bottom end feeding port of the second-stage hydrogenation reactor, the discharging end of the second-stage hydrogenation auxiliary pipeline is communicated with a middle feeding port of the second-stage hydrogenation reactor, a top discharging port of the second-stage hydrogenation reactor is communicated with a C4 product buffer tank after passing through the second-stage hydrogenation cooler, and the discharging end of the C4 product buffer tank is communicated with an OCC device after passing through a pressure regulating valve;
the C5 hydrogenation unit comprises a C5 raw material and a hydrogen raw material which are supplied from the outside of the device, the C5 raw material is communicated with the feed end of a C5 raw material buffer tank through a pipeline, the feed end of the C5 raw material buffer tank is provided with a liquid level regulating valve for controlling the liquid level, the discharge end of a C5 raw material buffer tank is communicated with a C5 raw material feed pump through a pipeline, the discharge end of a C5 raw material feed pump is communicated with a C5 raw material preheater, the discharge end of a C5 raw material feed pump is provided with a flow control valve, and the discharge end of a C5 raw material preheater is communicated with a C5 static mixer through a pipeline;
the C5 uses the hydrogen raw materials to link with C5 static mixer through the hydrogenation pipeline of C5, the discharge end of the C static mixer links with top of the hydrogenation reactor of C5, the bottom discharge end of the hydrogenation reactor of C5 links with C5 product surge tank after C5 hydrogenation cooler, the discharge end of the product surge tank of C5 is equipped with the pressure regulating valve and links with OCC device in parallel.
It should be noted that the C4 hydrogenation apparatus and the C5 hydrogenation apparatus have different raw materials and belong to the same inventive concept, the C4 raw material and the C5 raw material are both byproducts of MTO technology (methanol to olefin technology), which means that carbon chains in the MTO byproduct respectively have organic matters with 4 carbons and 5 carbons, and the C4 hydrogenation apparatus and the C5 hydrogenation apparatus have the function of performing hydrogenation reaction on dienes and alkynes in the C4 and C5 raw materials under the action of a catalyst, so that the content of monoolefins in the raw materials is increased, the coke formation amount of the OCC reaction is reduced, and the yield of the dienes is increased.
In order to improve the reasonability of the design and the convenience of application of the C4 hydrogenation device, the technical scheme provided by the invention also comprises a C4 discharge pipeline, wherein the discharge end of the section of hydrogenation reactor is directly communicated with the C4 product buffer tank, and a valve is arranged at the feed end of the C4 discharge pipeline. The design enables a first-section hydrogenation product at the discharge end of the first-section hydrogenation reactor to directly enter a C4 product buffer tank and discharge the product to enter a downstream OCC device without passing through a second-section hydrogenation reactor (controlled by a valve at the feed end of the first-section hydrogenation cooler and a valve at the feed end of a C4 discharge pipeline), so that a C4 raw material can be subjected to primary hydrogenation or secondary hydrogenation, and the use flexibility of the device is improved.
In order to improve the hydrogenation reaction effect of the C5 hydrogenation product and further improve the content of mono-olefin in the C5 hydrogenation product, the technical scheme of the invention also comprises that a pressure regulating valve is arranged at the discharge end of the C5 product buffer tank and communicated with a discharge pipeline I and a discharge pipeline II, and the discharge pipeline I is communicated with the OCC device; a discharge pipeline II is communicated with the feed end of the C5 static mixer through a C5 circulating pump, so that part of hydrogenated C5 products are pressurized by a C5 circulating pump and then return to the inlet of the C5 hydrogenation reactor to be mixed with fresh C5 raw materials for circular hydrogenation; the other part is directly sent to the downstream OCC device by the pressure of the other part.
The second purpose of the invention is to provide a hydrogenation method of a hydrogenation device for producing ethylene and propylene, which respectively comprises a C4 raw material hydrogenation method and a C5 raw material hydrogenation method;
the C4 raw material hydrogenation method comprises the following steps:
(1) hydrogen from the outside of the device enters a first-stage hydrogenation reactor and a second-stage hydrogenation reactor through a C4 hydrogenation pipeline respectively, wherein the hydrogen of the first-stage hydrogenation main pipeline enters from the feed end of a C4 static mixer I, the hydrogen of the first-stage hydrogenation auxiliary pipeline enters from the middle feed port of the first-stage hydrogenation reactor, the hydrogen of the second-stage hydrogenation main pipeline enters from the feed end of a C4 static mixer II, and the hydrogen of the second-stage hydrogenation auxiliary pipeline enters from the middle feed port of the second-stage hydrogenation reactor;
(2) the method comprises the following steps that a C4 raw material from the outside of a device enters a C4 raw material buffer tank under the control of a liquid level regulating valve, then a C4 raw material is pressurized by a C4 raw material feed pump (preferably to 2.1 MpaG) and is subjected to flow control, then the C4 raw material sequentially passes through a C4 condensation dehydrator, a C4 filter and a C4 raw material preheater and then enters a C4 static mixer I to be fully mixed with hydrogen, the mixed C4 raw material and hydrogen of a section of hydrogenation auxiliary pipeline enter a section of hydrogenation reactor and are subjected to hydrogenation reaction under the action of a catalyst to generate a section of hydrogenation reaction product, the section of hydrogenation reaction product comprises monoolefine olefins corresponding to a C4 raw material, namely butadiene and alkyne in the C4 raw material generate 1-butene under the action of the catalyst, and part of isomerization reaction;
(3) the first-stage hydrogenation reaction product is cooled by a first-stage hydrogenation cooler and then enters a C4 static mixer II to be fully mixed with hydrogen of a second-stage hydrogenation main pipeline, the mixed first-stage hydrogenation reaction product and hydrogen of a second-stage hydrogenation auxiliary pipeline enter a second-stage hydrogenation reactor to be subjected to hydrogenation reaction under the action of a catalyst to generate a second-stage hydrogenation reaction product, the second-stage hydrogenation reaction product is mono-olefin corresponding to a C4 raw material, namely butadiene and alkyne in the C4 raw material generate 1-butene under the action of the catalyst, and part of isomerization reaction generates cis-butene and trans-2-butene;
(4) cooling the second-stage hydrogenation reaction product by a second-stage hydrogenation cooler, then feeding the cooled second-stage hydrogenation reaction product into a C4 product buffer tank for first-stage flash evaporation, and then feeding the second-stage hydrogenation reaction product into a downstream OCC device;
the C5 raw material hydrogenation method comprises the following steps:
(1) hydrogen from the outside of the device enters a C5 static mixer through a C5 hydrogenation pipeline;
(2) the method comprises the steps of enabling a C5 raw material from a device to enter a C5 raw material buffer tank under the control of a liquid level regulating valve, enabling the C5 raw material to enter a C5 raw material preheater after being pressurized (preferably to 2.1 MpaG) and controlled by a C5 raw material feed pump, enabling a preheated C5 raw material to enter a C5 static mixer to be fully mixed with hydrogen, enabling the mixed C5 raw material and the hydrogen to enter a C5 hydrogenation reactor and react under the action of a catalyst to generate a C5 hydrogenation reaction product of corresponding mono-olefin, namely enabling diene and alkyne in the C5 raw material to generate mono-olefin under the action of the catalyst.
(3) And discharging a C5 hydrogenation reaction product from the bottom end of the C5 hydrogenation reactor, cooling the product by a C5 hydrogenation cooler, entering a C5 product buffer tank for primary flash evaporation, and then sending the product to a downstream OCC device.
In the step (2) of the hydrogenation method for the C4 raw material, the first-stage hydrogenation reaction product discharged from the first-stage hydrogenation reactor is directly conveyed to a C4 product buffer tank through a C4 discharge pipeline for first-stage flash evaporation, and then is conveyed to a downstream OCC device without passing through a second-stage hydrogenation reactor, so that the use flexibility of the device is improved.
In the step (3) of the C5 hydrogenation method, after flash evaporation through a C5 product buffer tank, one part of a C5 hydrogenation reaction product is pressurized through a C5 circulating pump and then is conveyed to the feed end of a C5 static mixer for circulation, and the other part of the C5 hydrogenation reaction product is conveyed to a downstream OCC device, so that the C5 hydrogenation reaction is more complete through circulating hydrogen addition, and the contents of dialkene and alkyne are reduced to the maximum extent.
The invention has the beneficial effects that: compared with the prior art, the invention aims to provide a hydrogenation device and a hydrogenation method for producing ethylene and propylene, which can effectively reduce the contents of dialkenes and alkynes in C4 and C5 raw materials in an OCC device, improve the content of monoolefins in C4 and C5 raw materials, and further improve the yield of diene, and in order to realize the technical effects:
firstly, through a C4 hydrogenation device, a C4 raw material is fully mixed with hydrogen in a C4 static mixer after passing through equipment such as a C4 raw material buffer tank, a C4 raw material preheater and the like in sequence, and then enters a first-stage hydrogenation reactor and a second-stage hydrogenation reactor in sequence, and is subjected to hydrogenation reaction with the hydrogen under the action of a catalyst, so that butadiene and alkyne in the C4 raw material generate 1-butene under the action of the catalyst, part of isomerization reaction generates cis-butene and trans-2-butene, diene and alkyne in the C4 raw material are removed, and then the diene and alkyne enter a downstream OCC device, thereby preventing the polymerization of the butadiene and the alkyne from blocking a pore channel of the catalyst in the downstream OCC reactor, reducing the coke formation amount, prolonging the switching period of the reactor, further improving the yield of target products (ethylene and propylene), and improving the economic benefit of the device;
secondly, the C5 hydrogenation device is adopted, so that a C5 raw material sequentially passes through a C5 raw material buffer tank, a C5 raw material preheater and other devices, then enters a C5 static mixer to be mixed with hydrogen, and then enters a C5 hydrogenation reactor to carry out hydrogenation reaction under the action of a catalyst, so that dialkenes and alkynes in a C5 raw material generate corresponding mono-olefins under the action of the catalyst, and then enter a downstream OCC device, the same technical effect as that of the C4 hydrogenation device is achieved, the situation that pore passages of the catalyst in the downstream OCC reactor are blocked by polymerization of the dialkenes and alkynes in the C5 raw material is avoided, the coke production is reduced, the switching period of the reactor is prolonged, the yield of target products (ethylene and propylene) of the OCC device is further improved, and the economic benefit of the device;
finally, the hydrogenation device and the hydrogenation method of the invention are tested by actual production, the content of dialkene and alkyne before hydrogenation of the C4 raw material is 1.56wt%, the content of dialkene is 0wt% after hydrogenation reaction, and the content of monoolefine is increased; c5 the content of dialkene and alkyne before hydrogenation of raw material is 5.18%, the content of dialkene and alkyne after hydrogenation is 0wt%, the content of mono-olefin is increased; actual production data shows that C4 and C5 raw materials are subjected to hydrogenation reaction by the device before catalytic cracking reaction, so that dialkene and alkyne are completely removed, and the content of monoolefine after hydrogenation is higher than that before hydrogenation, which is beneficial to reducing the coke formation amount of the reaction and improving the diene yield of the OCC device.
Drawings
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present invention, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained based on these drawings without creative efforts.
FIG. 1 is a diagram of a C4 hydrogenation apparatus and a hydrogenation scheme in an embodiment.
FIG. 2 is a diagram of a C5 hydrogenation apparatus and hydrogenation scheme in an embodiment.
The system comprises a first-stage hydrogenation reactor 1, a second-stage hydrogenation reactor 2, a first-stage hydrogenation main pipeline 3, a C4 static mixer I4, a first-stage hydrogenation auxiliary pipeline 5, a second-stage hydrogenation main pipeline 6, a C4 static mixer II 7, a second-stage hydrogenation auxiliary pipeline 8, a liquid level regulating valve 9, a C4 raw material buffer tank 10, a C4 raw material feed pump 11, a C4 condensation dehydrator 12, a C4 filter 13, a C4 raw material preheater 14, a C4 discharge pipeline 15, a C4 discharge pipeline 16, a C4 product buffer tank 17, an OCC device 18, a first-stage hydrogenation cooler 19, a C5 static mixer 20, a C5 raw material buffer tank 21, a C5 raw material feed pump 22, a C5 raw material preheater 23, a C5 hydrogenation reactor 24, a C5 hydrogenation cooler 25, a C5 product buffer tank 26, a C5 circulating pump 27 and a valve 28.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the present invention, the technical solution in the embodiment of the present invention will be clearly and completely described below with reference to the drawings in the embodiment of the present invention, and it is obvious that the described embodiment is only a part of the embodiment of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "center", "lateral", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are used for descriptive purposes only to simplify the description of the present invention, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and therefore, are not to be construed as limiting the present invention.
As can be seen from the attached drawing, the hydrogenation device and the hydrogenation method for producing ethylene and propylene comprise a C4 raw material hydrogenation device and a C5 raw material hydrogenation method;
the C4 raw material hydrogenation device and the method comprise the following steps:
(1) hydrogen from the outside of the device enters a first-stage hydrogenation reactor 1 and a second-stage hydrogenation reactor 2 through a C4 hydrogenation pipeline respectively, wherein the hydrogen of a first-stage hydrogenation main pipeline 3 enters from the feed end of a C4 static mixer I4, the hydrogen of a first-stage hydrogenation auxiliary pipeline 5 enters from the middle feed port of the first-stage hydrogenation reactor 1, the hydrogen of a second-stage hydrogenation main pipeline 6 enters from the feed end of a C4 static mixer II 7, and the hydrogen of a second-stage hydrogenation auxiliary pipeline 8 enters from the middle feed port of the second-stage hydrogenation reactor 2;
(2) the method comprises the following steps that a C4 raw material from the outside of a device enters a C4 raw material buffer tank 10 under the control of a liquid level regulating valve 9, then a C4 raw material is pressurized and controlled by a C4 raw material feed pump 11, then sequentially passes through a C4 condensation dehydrator 12, a C4 filter 13 and a C4 raw material preheater 14, then enters a C4 static mixer I4 to be fully mixed with hydrogen, the mixed C4 raw material and hydrogen enter a first-section hydrogenation reactor 1 together with hydrogen of a first-section hydrogenation auxiliary pipeline 5, and are subjected to hydrogenation reaction under the action of a catalyst to generate a first-section hydrogenation reaction product, wherein the first-section hydrogenation reaction product comprises mono-olefins corresponding to the C4; in addition, a first-stage hydrogenation reaction product discharged from the first-stage hydrogenation reactor 1 can be directly conveyed to a C4 product buffer tank 17 through a C4 discharge pipeline 16 for first-stage flash evaporation, then is conveyed to a downstream OCC device 18, and is subjected to first-stage hydrogenation without passing through the second-stage hydrogenation reactor 2 by controlling a corresponding valve 28, so that the use flexibility of the device is improved;
(3) the first-stage hydrogenation reaction product is cooled by a first-stage hydrogenation cooler 19, enters a C4 static mixer II 7 and is fully mixed with hydrogen of a second-stage hydrogenation main pipeline 6, the mixed first-stage hydrogenation reaction product and hydrogen of a second-stage hydrogenation auxiliary pipeline 8 enter a second-stage hydrogenation reactor 2 and are subjected to hydrogenation reaction under the action of a catalyst to generate a second-stage hydrogenation reaction product, and the second-stage hydrogenation reaction product is mono-olefin corresponding to a C4 raw material;
(4) the second-stage hydrogenation reaction product is cooled by a second-stage hydrogenation cooler 15, enters a C4 product buffer tank 17 for first-stage flash evaporation, and then is sent to a downstream OCC device 18;
the C5 raw material hydrogenation device and the method comprise the following steps:
(1) hydrogen from the outside of the unit enters the C5 static mixer 20 through a C5 hydrogenation line;
(2) c5 raw material from the device enters a C5 raw material buffer tank 21 under the control of a liquid level regulating valve 9, then C5 raw material enters a C5 raw material preheater 23 after being pressurized and controlled by a C5 raw material feed pump 22 and the preheated C5 raw material enters a C5 static mixer 20 to be fully mixed with hydrogen, and the mixed C5 raw material and hydrogen enter a C5 hydrogenation reactor 24 to react under the action of a catalyst to generate a C5 hydrogenation reaction product of corresponding mono-olefin;
(3) c5 hydrogenation reaction products are discharged from the bottom end of a C5 hydrogenation reactor 24, cooled by a C5 hydrogenation cooler 25, enter a C5 product buffer tank 26 for primary flash evaporation, after flash evaporation of the C5 product buffer tank 26, a part of the C5 hydrogenation reaction products are pressurized by a C5 circulating pump 27 and then are conveyed to the feed end of a C5 static mixer 20 for circulation, and the other part of the C5 hydrogenation reaction products are conveyed to a downstream OCC device 18.
The application discloses a hydrogenation device for producing ethylene propylene and a corresponding hydrogenation method, a C4 raw material and a C5 raw material are subjected to selective hydrogenation reaction under the action of a catalyst, diene and alkyne in a C4 raw material and a C5 raw material can be effectively converted into mono-olefin, the diene and alkyne in the C4 and C5 raw materials can be completely removed, the content of the mono-olefin in the raw material is increased while the diene and alkyne in the raw material are removed, the phenomenon that the pore passages of the catalyst in a downstream OCC device reactor are blocked by polymerization of diene and alkyne components is avoided, the coke formation amount of the OCC reaction is reduced, the switching period of the reactor is prolonged, and the yield of the diene is improved.
Although the present invention has been described in detail by referring to the drawings in connection with the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and scope of the present invention, and these modifications or substitutions are within the scope of the present invention/any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.
Claims (6)
1. A hydrogenation device for producing ethylene and propylene is characterized in that: the hydrogenation system comprises a C4 hydrogenation device and a C5 hydrogenation device, wherein the C4 hydrogenation device comprises a C4 raw material and a hydrogen raw material, and the hydrogen raw material is respectively communicated with a first-stage hydrogenation reactor and a second-stage hydrogenation reactor through a C4 hydrogenation pipeline; the C4 raw material is communicated with a feed end of a C4 raw material buffer tank through a pipeline, a liquid level regulating valve is arranged at the feed end of a C4 raw material buffer tank, a discharge end of a C4 raw material buffer tank is communicated with a C4 raw material feed pump through a pipeline, a discharge end of a C4 raw material feed pump is communicated with a feed end of a C4 static mixer I through a C4 condensation dehydrator, a C4 filter and a C4 raw material preheater which are sequentially communicated, a discharge end of the C4 raw material feed pump is provided with a flow control valve, and a discharge end of the C4 static mixer I is communicated with a bottom feed inlet of a section of hydrogenation reactor; the C4 hydrogenation pipeline comprises a first section of hydrogenation main pipeline, a first section of hydrogenation auxiliary pipeline, a second section of hydrogenation main pipeline and a second section of hydrogenation auxiliary pipeline which are arranged in parallel and provided with valves, the discharge end of the first section of hydrogenation main pipeline is communicated with the feed end of the C4 static mixer I, the discharge end of the first section of hydrogenation auxiliary pipeline is communicated with the middle feed inlet of the first section of hydrogenation reactor, and the top discharge port of the first section of hydrogenation reactor is communicated with a first section of hydrogenation cooler through a pipeline; a valve is arranged at the feeding end of the first-stage hydrogenation cooler, the discharging end of the first-stage hydrogenation cooler and the discharging end of the second-stage hydrogenation main pipeline are communicated with a C4 static mixer II through pipelines, the discharging end of the C4 static mixer II is communicated with a bottom end feeding port of the second-stage hydrogenation reactor, the discharging end of the second-stage hydrogenation auxiliary pipeline is communicated with a middle feeding port of the second-stage hydrogenation reactor, a top discharging port of the second-stage hydrogenation reactor is communicated with a C4 product buffer tank after passing through the second-stage hydrogenation cooler, and the discharging end of the C4 product buffer tank is communicated with an OCC device after passing through a pressure regulating valve;
the C5 hydrogenation device comprises a C5 raw material and a hydrogen raw material, wherein the C5 raw material is communicated with a feeding end of a C5 raw material buffer tank through a pipeline, a liquid level regulating valve is arranged at the feeding end of the C5 raw material buffer tank, a C5 raw material feeding pump is communicated with a discharging end of a C5 raw material buffer tank through a pipeline, a C5 raw material preheater is communicated with a discharging end of a C5 raw material feeding pump, a flow control valve is arranged at the discharging end of a C5 raw material feeding pump, a C5 static mixer is communicated with the discharging end of the C5 raw material preheater through a pipeline, the hydrogen raw material is communicated with a C5 static mixer through a C5 hydrogenation pipeline, the discharging end of the C5 static mixer is communicated with the top end of a C5 hydrogenation reactor, the discharging end of the bottom of the C5 hydrogenation reactor is communicated with a C5 product buffer tank through a C5 hydrogenation cooler, and a pressure regulating valve is arranged at the discharging end of a C5 product buffer.
2. The hydrogenation apparatus for producing ethylene and propylene according to claim 1, wherein: the discharge end of the first section of the hydrogenation reactor is directly communicated with a C4 discharge pipeline of a C4 product buffer tank, and the feed end of the C4 discharge pipeline is provided with a valve.
3. The hydrogenation apparatus for producing ethylene and propylene according to claim 1, wherein: the discharge end of C5 product buffer tank is equipped with pressure regulating valve and parallelly connected to have discharge pipeline I and discharge pipeline II, discharge pipeline I and OCC device UNICOM, discharge pipeline II through the feed end UNICOM of C5 circulating pump with C5 static mixer.
4. A hydrogenation method suitable for the hydrogenation device for producing ethylene and propylene, which comprises a C4 raw material hydrogenation method and a C5 raw material hydrogenation method;
the C4 raw material hydrogenation method comprises the following steps:
(1) hydrogen from the outside of the device enters a first-stage hydrogenation reactor and a second-stage hydrogenation reactor through a C4 hydrogenation pipeline respectively, wherein the hydrogen of the first-stage hydrogenation main pipeline enters from the feed end of a C4 static mixer I, the hydrogen of the first-stage hydrogenation auxiliary pipeline enters from the middle feed port of the first-stage hydrogenation reactor, the hydrogen of the second-stage hydrogenation main pipeline enters from the feed end of a C4 static mixer II, and the hydrogen of the second-stage hydrogenation auxiliary pipeline enters from the middle feed port of the second-stage hydrogenation reactor;
(2) c4 raw materials from the outside of the device enter a C4 raw material buffer tank under the control of a liquid level regulating valve, then C4 raw materials are pressurized and controlled by a C4 raw material feed pump, pass through a C4 condensation dehydrator, a C4 filter and a C4 raw material preheater in sequence, enter a C4 static mixer I and are fully mixed with hydrogen, the mixed C4 raw materials and the hydrogen enter a section of hydrogenation reactor together with hydrogen of a section of hydrogenation auxiliary pipeline, and are subjected to hydrogenation reaction under the action of a catalyst to generate a section of hydrogenation reaction product, wherein the section of hydrogenation reaction product comprises monoolefin corresponding to a C4 raw material;
(3) the first-stage hydrogenation reaction product is cooled by a first-stage hydrogenation cooler and then enters a C4 static mixer II, and is fully mixed with hydrogen of a second-stage hydrogenation main pipeline, the mixed first-stage hydrogenation reaction product and hydrogen of a second-stage hydrogenation auxiliary pipeline enter a second-stage hydrogenation reactor and are subjected to hydrogenation reaction under the action of a catalyst, so that a second-stage hydrogenation reaction product is generated, and the second-stage hydrogenation reaction product is mono-olefin corresponding to a C4 raw material;
(4) cooling the second-stage hydrogenation reaction product by a second-stage hydrogenation cooler, then feeding the cooled second-stage hydrogenation reaction product into a C4 product buffer tank for first-stage flash evaporation, and then feeding the second-stage hydrogenation reaction product into a downstream OCC device;
the C5 raw material hydrogenation method comprises the following steps:
(1) hydrogen from the outside of the device enters a C5 static mixer through a C5 hydrogenation pipeline;
(2) the method comprises the following steps that C5 raw material from the outside of the device enters a C5 raw material buffer tank under the control of a liquid level regulating valve, then C5 raw material enters a C5 raw material preheater after being pressurized and controlled by a C5 raw material feed pump, preheated C5 raw material enters a C5 static mixer to be fully mixed with hydrogen, and the mixed C5 raw material and hydrogen enter a C5 hydrogenation reactor to react under the action of a catalyst to generate a C5 hydrogenation reaction product of corresponding mono-olefin;
(3) and discharging a C5 hydrogenation reaction product from the bottom end of the C5 hydrogenation reactor, cooling the product by a C5 hydrogenation cooler, entering a C5 product buffer tank for primary flash evaporation, and then sending the product to a downstream OCC device.
5. The hydrogenation method of a hydrogenation unit for producing ethylene and propylene according to claim 4, wherein: in the step (2) of the C4 raw material hydrogenation method, a first-stage hydrogenation reaction product discharged from a first-stage hydrogenation reactor is directly conveyed to a C4 product buffer tank through a C4 discharge pipeline for first-stage flash evaporation, and then is conveyed to a downstream OCC device.
6. The hydrogenation method of a hydrogenation unit for producing ethylene and propylene according to claim 4, wherein: in the step (3) of the C5 hydrogenation method, after the flash evaporation of the C5 product buffer tank, one part of the C5 hydrogenation reaction product is pressurized by a C5 circulating pump and then is conveyed to the feed end of a C5 static mixer for circulation, and the other part of the C5 hydrogenation reaction product is conveyed to a downstream OCC device.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114253238A (en) * | 2021-12-14 | 2022-03-29 | 浙江中控技术股份有限公司 | License plate switching method and device, electronic equipment and storage medium |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6049017A (en) * | 1998-04-13 | 2000-04-11 | Uop Llc | Enhanced light olefin production |
| CN101045665A (en) * | 2006-03-27 | 2007-10-03 | 中国石油化工股份有限公司 | Method for producing propylene from carbon-contained alkene by catalytic cracking |
| CN105367366A (en) * | 2014-08-27 | 2016-03-02 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by means of mixed C4 |
| CN106866329A (en) * | 2017-01-22 | 2017-06-20 | 江苏天诺新材料科技股份有限公司 | The preparation method of low-carbon alkene |
| CN109369318A (en) * | 2018-12-07 | 2019-02-22 | 宁波旭合瑞石化工程有限公司 | A method of the raw material based on C5 alkene maximizes production propylene |
-
2020
- 2020-04-01 CN CN202010249488.7A patent/CN111233613A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6049017A (en) * | 1998-04-13 | 2000-04-11 | Uop Llc | Enhanced light olefin production |
| CN101045665A (en) * | 2006-03-27 | 2007-10-03 | 中国石油化工股份有限公司 | Method for producing propylene from carbon-contained alkene by catalytic cracking |
| CN105367366A (en) * | 2014-08-27 | 2016-03-02 | 中国石油化工股份有限公司 | Method for producing ethylene and propylene by means of mixed C4 |
| CN106866329A (en) * | 2017-01-22 | 2017-06-20 | 江苏天诺新材料科技股份有限公司 | The preparation method of low-carbon alkene |
| CN109369318A (en) * | 2018-12-07 | 2019-02-22 | 宁波旭合瑞石化工程有限公司 | A method of the raw material based on C5 alkene maximizes production propylene |
Non-Patent Citations (1)
| Title |
|---|
| 滕加伟: "烯烃催化裂解增产丙烯技术(OCC)" * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114253238A (en) * | 2021-12-14 | 2022-03-29 | 浙江中控技术股份有限公司 | License plate switching method and device, electronic equipment and storage medium |
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