CN115894145A - Propane dehydrogenation process - Google Patents
Propane dehydrogenation process Download PDFInfo
- Publication number
- CN115894145A CN115894145A CN202211333107.9A CN202211333107A CN115894145A CN 115894145 A CN115894145 A CN 115894145A CN 202211333107 A CN202211333107 A CN 202211333107A CN 115894145 A CN115894145 A CN 115894145A
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- tube
- reactor
- heating furnace
- propane dehydrogenation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 58
- 239000001294 propane Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 37
- 239000002994 raw material Substances 0.000 claims abstract description 65
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 37
- 239000002918 waste heat Substances 0.000 claims abstract description 13
- 238000010438 heat treatment Methods 0.000 claims description 58
- 238000011010 flushing procedure Methods 0.000 claims description 36
- 238000004804 winding Methods 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 11
- 238000003466 welding Methods 0.000 claims description 6
- 239000000047 product Substances 0.000 abstract description 12
- 238000001816 cooling Methods 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 238000004064 recycling Methods 0.000 abstract 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 10
- 229910052739 hydrogen Inorganic materials 0.000 description 10
- 239000001257 hydrogen Substances 0.000 description 10
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 8
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000012530 fluid Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000007667 floating Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- -1 carbon ion Chemical class 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000003849 aromatic solvent Substances 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/26—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only halogen atoms as hetero-atoms
- C07C1/30—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only halogen atoms as hetero-atoms by splitting-off the elements of hydrogen halide from a single molecule
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
- F28F9/02—Header boxes; End plates
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28G—CLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
- F28G9/00—Cleaning by flushing or washing, e.g. with chemical solvents
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of propane dehydrogenation, and particularly relates to a propane dehydrogenation process. The process utilizes the waste heat of the reaction product to heat the reaction raw material, thereby effectively recycling the waste heat of the reaction product, effectively reducing the problem of temperature rise energy consumption of the reaction product, and reducing the problem of high product temperature and large cooling load.
Description
Technical Field
The invention belongs to the technical field of propane dehydrogenation, and particularly relates to a propane dehydrogenation process.
Background
Propylene is an important organic chemical raw material and has the characteristics of wide application, large market demand and the like. In recent years, demand for propylene has been increasing rapidly in various industries such as chemical industry and manufacturing industry. Due to the increase of the demand of propylene, the related processes of propane dehydrogenation, propylene preparation and the like are continuously and vigorously developed.
Propane dehydrogenation is a method for producing propylene monomer by propane dehydrogenation, and is an important method for producing propylene, and the production of propylene from propane requires treatment of a dehydrogenation device. At present, because propane dehydrogenation needs to be carried out at a higher temperature, the energy consumption of propane dehydrogenation is high, and the cost is high; the conventional propane dehydrogenation device needs a heat exchanger for feeding and discharging materials, a floating head heat exchanger is often adopted, the structure is complex, a small cover at the floating head end cannot be checked in operation, the sealing requirement is high, the material consumption is high in the start-up process, a tube bundle is easy to crack, the heat exchange effect is poor, the load of heating in the subsequent reaction of propane dehydrogenation is increased, and the heating time is long; meanwhile, the temperature of the product obtained by propane dehydrogenation is higher, the product can enter the next system after being cooled, and the product temperature is higher, so that the cooling load is larger and the cooling time is long.
Therefore, the propane dehydrogenation process is costly and inefficient, severely hampering propylene production, for the reasons described above.
Disclosure of Invention
Aiming at the technical problems at present, the invention provides a propane dehydrogenation process, wherein heat exchange is carried out in the process, a wound tube type heat exchanger is selected for heat exchange, the heat exchange effect is good, the load of a subsequent heating furnace is reduced, meanwhile, the reaction raw material is heated by utilizing the waste heat of a reaction product, the waste heat of the reaction product is effectively recycled, the problem of temperature rise energy consumption of the reaction product is effectively reduced, the problem of high product temperature and large cooling load is reduced, the cost of propane dehydrogenation is effectively reduced, and the efficiency is improved.
The technical scheme of the invention is as follows:
a propane dehydrogenation process utilizes a propane dehydrogenation system, and comprises the steps that raw materials enter a reactor to react after being heated to obtain reaction products, the reaction products are gathered into a subsequent treatment system, and the heating process firstly utilizes the waste heat of the reaction products to exchange heat with the raw materials in a wound tube type heat exchanger, then the raw materials are heated by a heating furnace, and then the raw materials enter the reactor to react.
Preferably, the raw materials are subjected to heat exchange in the wound tube type heat exchanger and heated by the heating furnace and then enter the reactor for reaction, the obtained reaction product is heated by another heating furnace and then enters another reactor for reaction, the obtained reaction product is heated by the next heating furnace and then enters another reactor for reaction, and the obtained reaction product and the raw materials are subjected to heat exchange in the wound tube type heat exchanger and then converge into a subsequent treatment system. Propane dehydrogenation is an endothermic process, a large amount of heat is needed in dehydrogenation reaction, if only one set of dehydrogenation reaction is needed, the dehydrogenation reaction is incomplete, the problems of raw material waste, low conversion rate, low yield and the like can be caused, and the conversion rate can be improved and the yield is improved by adding three sets of dehydrogenation reaction.
Preferably, the raw materials are cooled and then heated, and finally enter a wound tube type heat exchanger to exchange heat with the reaction product. The raw material is cooled firstly to remove hydrogen in the raw material, and the existence of hydrogen can cause serious defects to steel, such as: hydrogen embrittlement, hydrogen corrosion, cracks of a heat affected zone of a welding seam and the like, and the existence of hydrogen in raw materials is not beneficial to the dehydrogenation reaction. If the raw materials after cooling directly get into winding tubular heat exchanger, the difference in temperature of intensification is great, and the energy further increase that needs to provide will be very high so whole device's energy consumption, uneconomic, and the raw materials after the cooling is earlier little amplitude's intensification simultaneously also makes the raw materials can the thermally equivalent, has avoided being heated uneven problem.
Preferably, the propane dehydrogenation system comprises a raw material storage tank, a wound tube type heat exchanger, a reactor and a heating furnace; the raw material storage tank is sequentially connected with a raw material cooler, a cold feeding heat exchanger, a tube side of a wound tube type heat exchanger, a heating furnace, a reactor, a shell side of the wound tube type heat exchanger and a subsequent treatment system.
Further preferably, a raw material cooler and a cold feed heat exchanger are arranged between the raw material storage tank and the wound tube heat exchanger.
Further preferably, the reactor comprises a first reactor, a second reactor and a third reactor, and the heating furnace comprises a first heating furnace, a second heating furnace and a third heating furnace; and the tube side outlet of the winding tube type heat exchanger is sequentially connected with a first heating furnace, a first reactor, a second heating furnace, a second reactor, a third heating furnace, a third reactor and a shell side inlet of the heat exchanger.
Further preferably, holes are formed in the tube plate of the wound tube type heat exchanger, the holes are arranged in a regular triangle shape, the high-temperature end (the high-temperature end is close to the tube pass outlet) of the tube plate is connected with the heat exchange tube on the wound tube type heat exchanger through deep hole welding, and the heat exchange tube is communicated with the holes in the tube plate. The tube plates are regularly triangular in arrangement, the maximum number of tubes can be arranged on the same area of the tube plates in an arrangement mode of regular triangles, the arrangement is compact, and tube pass fluid directly scours the heat exchange tubes, so that the tube pass fluid is more uniformly distributed; the high-temperature end of the tube plate is easy to generate carbon ion aggregation, and the aggregation extrudes and deforms the heat exchange tube, so that the problem is avoided by adopting deep hole welding. Further preferably, the hole spacing on the tube plate is 22mm, the adopted spacing is small, a plurality of tubes can be arranged, and the size of the tube plate is reduced.
Further preferably, flushing pipes are wound above and below the outer side of the shell of the wound tube type heat exchanger, openings A are uniformly formed in the flushing pipes, an opening B is formed in the position, corresponding to the opening A, of the shell of the wound tube type heat exchanger, the opening A in the flushing pipe is connected with the opening B in the shell, the flushing pipe is connected with a flushing pipeline, and a valve is arranged on the flushing pipeline; and openings C are formed in the tube side inlet and the tube side outlet of the wound tube type heat exchanger, the shell side inlet and the shell side outlet of the wound tube type heat exchanger and are connected with a flushing pipeline, and valves are arranged on the flushing pipeline. Propane dehydrogenation is an endothermic reaction, which requires high energy supplied from the outside, and the reaction is limited by thermodynamic equilibrium, and needs to obtain high conversion rate at high temperature, but floccules are easy to generate at medium temperature (150-200 ℃), so that openings need to be added in the shell and at each inlet and outlet for easy flushing.
The inlet of the shell of the wound tube type heat exchanger is provided with the impingement plate, so that the heat exchange tube in the wound tube type heat exchanger is prevented from being directly washed by fluid to cause vibration instability and corrosion of the heat exchange tube.
According to the invention, the raw material is heated to a certain temperature by the heat exchanger, enters the heating furnace, is heated by the heating furnace and enters the reactor for reaction, the temperature of a reaction product discharged from the reactor is higher, and then the reaction product is introduced into the heat exchanger to exchange heat with the raw material, and the reaction product after heat exchange enters a subsequent treatment system or a collection device. The winding tube type heat exchanger is selected, so that the heat exchange effect is good, the load of a subsequent heating furnace is reduced, meanwhile, the reaction raw material is heated by utilizing the waste heat of the reaction product, heat can be provided for the raw material, the waste heat of the reaction product is effectively recycled, the temperature of the reaction product is effectively reduced, the problem that the reaction raw material needs high energy consumption for heating is reduced, and the problem that the product temperature is high and the cooling load is large is reduced; after the original floating head heat exchanger is replaced by a wound tube heat exchanger, the tube shell process materials are exchanged, so that the process requirements can be met; through the system, the cost of propane dehydrogenation is effectively reduced, and the production efficiency is improved.
Drawings
FIG. 1 is a schematic structural view of the process of the present invention;
FIG. 2 is a schematic diagram of a wound tube heat exchanger according to the present invention;
FIG. 3 is a schematic structural view of a tube sheet of a wound tube heat exchanger;
FIG. 4 is a regular triangular arrangement of the holes in the tube sheet of the wound tube heat exchanger;
FIG. 5 is a schematic structural diagram of a tube sheet and a heat exchange tube of a wound tube heat exchanger;
FIG. 6 is a schematic view of the structure of the joint between the tube plate and the heat exchange tube of the wound tube heat exchanger;
FIG. 7 is a schematic view of the connection of the impingement plate to the shell side inlet;
FIG. 8 is a schematic view of the impingement plate;
in the figure, 1 is a raw material storage tank, 2 is a raw material cooler, 3 is a cold feed heat exchanger, 4 is a wound tube heat exchanger, 4-1 is a tube side outlet, 4-2 is a tube side inlet, 4-3 is a shell side outlet, 4-4 is a shell side inlet, 4-5 is an opening C,4-6 is a tube plate, 4-7 is a flushing tube, 4-8 is a heat exchange tube, 4-9 is an impingement plate, 5 is a heating furnace, 5-1 is a first heating furnace, 5-2 is a second heating furnace, 5-3 is a third heating furnace, 6 is a reactor, 6-1 is a first reactor, 6-2 is a second reactor, 6-3 is a third reactor, and 7 is a subsequent treatment system.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly described below, and it is obvious that the described embodiments are a part of the embodiments of the present invention, but not all of the 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.
As shown in the figure, the propane dehydrogenation process utilizes a propane dehydrogenation system, and comprises the steps that raw materials are heated and then enter a reactor 6 to obtain a reaction product, and the reaction product enters the shell pass of a wound tube type heat exchanger 4 and finally flows into a subsequent treatment system 7; in the temperature rising process, the waste heat of the reaction product and the raw materials are firstly utilized to exchange heat in the winding tube type heat exchanger 4, then are heated by the heating furnace 5, and then enter the reactor 6 for reaction.
In the invention, after the original floating head heat exchanger in the prior art is replaced by the winding tube type heat exchanger 4, the tube shell side material is exchanged, the process requirement can be met, the allowable pressure drop of the tube side in the process file is required to be 13.8Kpa, and if the tube side is not exchanged, the calculated pressure drop of the tube side is 21.86Kpa, which is not in accordance with the requirement. According to the invention, the winding tube type heat exchanger 4 is selected, the heat exchange effect is good, the load of the subsequent heating furnace 5 is reduced, the reaction raw material is heated by utilizing the waste heat of the reaction product, the heat can be provided for the raw material, the waste heat of the reaction product is effectively recycled, the temperature of the reaction product is effectively reduced, the problem that the reaction raw material needs to be heated by higher energy consumption is reduced, the problem that the product temperature is high and the cooling load is large is reduced, and the cost of propane dehydrogenation is effectively reduced.
In the winding tube type heat exchanger 4, the heat exchange tubes 4-8 are alternately wound in a spiral shape in the space between the central tube and the outer shell, the winding directions of the adjacent two layers of heat exchange tubes 4-8 are opposite, and a certain distance is kept by adopting a certain shape of distance piece.
In another embodiment, the raw materials are subjected to heat exchange in the wound tube type heat exchanger 4, heated by the heating furnace 5 and then enter the reactor 6 for reaction, the obtained reaction product is heated by the other heating furnace 5 and then enters the other reactor 6 for reaction, the obtained reaction product is heated by the next heating furnace 5 and then enters the other reactor 6 for reaction, and the obtained reaction product and the raw materials are subjected to heat exchange in the wound tube type heat exchanger 4 and then converge into a subsequent treatment system. Propane dehydrogenation is an endothermic process, a large amount of heat is needed in dehydrogenation reaction, if only one set of dehydrogenation reaction is needed, the dehydrogenation reaction is incomplete, the problems of raw material waste, low conversion rate, low yield and the like can be caused, three sets of dehydrogenation reaction are added, the conversion rate can be improved, and the yield is improved.
In another embodiment, the raw materials are cooled and then heated, and finally enter the wound tube heat exchanger 4 to exchange heat with the reaction product. The raw material is cooled firstly to remove hydrogen in the raw material, and the existence of hydrogen can cause serious defects to steel, such as: hydrogen embrittlement, hydrogen corrosion, cracks of a weld heat affected zone and the like, and the existence of hydrogen in the raw materials is not beneficial to the dehydrogenation reaction. If the raw materials after cooling directly get into winding tubular heat exchanger 4, the difference in temperature of intensification is great, and the energy further increase that needs to provide will be very high so whole device's energy consumption, uneconomic, and the raw materials after the cooling is earlier little amplitude intensification simultaneously also makes the raw materials can the thermally equivalent, has avoided being heated uneven problem.
The propane dehydrogenation system used in the propane dehydrogenation process comprises a raw material storage tank 1, a wound tube type heat exchanger 4, a reactor 6 and a heating furnace 5; the raw material storage tank 1 is sequentially connected with a raw material cooler 2, a cold feeding heat exchanger 3, a tube pass of a wound tube type heat exchanger 4, a heating furnace 5, a reactor 6, a shell pass of the wound tube type heat exchanger 4 and a subsequent treatment system 7.
The other is the implementation mode, the upper part and the lower part of the outer side of the shell of the wound tube type heat exchanger 4 are respectively wound with flushing pipes 4-7, the flushing pipes 4-7 are uniformly provided with openings A, the shell position of the wound tube type heat exchanger 4 corresponding to the openings A is provided with openings B, the openings A on the flushing pipes 4-7 are connected with the openings B on the shell (so that flushing liquid can enter the openings A through the flushing pipes 4-7 and then enter the shell through the openings B), the flushing pipes 4-7 are connected with a flushing pipeline, and valves are arranged on the flushing pipeline; the tube side outlet 4-1, the tube side inlet 4-2, the shell side outlet 4-3 and the shell side inlet 4-4 of the winding tube type heat exchanger 4 are all provided with openings C4-5, the openings are connected with a flushing pipeline, and the flushing pipeline is provided with a valve. Propane dehydrogenation is an endothermic reaction, which requires high external energy, and the reaction is limited by thermodynamic equilibrium, and needs to be carried out at a high temperature to obtain a high conversion rate, but floccules are easily generated in a medium-temperature section (150-200 ℃), so that openings need to be added in the shell and at each inlet and outlet to facilitate flushing. Flushing pipes 4-7 on the casing can be washed (i.e. washed in the process of operation) on line and also can be washed out in a shutdown way, and when the flushing is carried out on line, the flushing liquid selects an aromatic solvent, and in the process of washing on line, the flushing liquid is incompatible with light components (products), so that the flushing liquid cannot influence the products, and the flushing at each inlet and outlet needs to be carried out in a shutdown way for flushing.
The other way is that the baffle 4-9 is arranged at the shell side inlet 4-4 of the wound tube type heat exchanger 4 to prevent the fluid from directly scouring the heat exchange tubes 4-8 in the wound tube type heat exchanger 4 to cause the vibration instability and corrosion of the heat exchange tubes 4-8. The impingement plate 4-9 is composed of an arc-shaped plate and four supporting columns, the four supporting columns are fixedly connected to the arc-shaped plate, the supporting columns are arranged on the back face of the arc-shaped plate in the bending direction, the four supporting columns are connected with the inlet of the shell, the arc-shaped plate is arranged in the shell, and a gap is formed between the arc-shaped plate and the winding pipe type heat exchanger 4.
The other way is that the implementation mode is that a raw material cooler 2 and a cold feeding heat exchanger 3 are arranged between the raw material storage tank 1 and the heat exchanger, and the cold feeding heat exchanger 3 adopts a plate heat exchanger; the reactor 6 comprises a first reactor 6-1, a second reactor 6-2 and a third reactor 6-3, and the heating furnace 5 comprises a first heating furnace 5-1, a second heating furnace 5-2 and a third heating furnace 5-3; the tube side outlet 4-1 of the heat exchanger is sequentially connected with a first heating furnace 5-1, a first reactor 6-1, a second heating furnace 5-2, a second reactor 6-2, a third heating furnace 5-3 and a third reactor 6-3, and the shell side inlet 4-4 of the wound tube type heat exchanger 4. The raw materials are cooled and heated, enter a tube pass of a winding tube type heat exchanger 4, sequentially pass through a first heating furnace 5-1, a first reactor 6-1, a second heating furnace 5-2, a second reactor 6-2, a third heating furnace 5-3 and a third reactor 6-3, and finally obtain a reaction product, enter a shell pass of the winding tube type heat exchanger 4 and finally flow into a subsequent treatment system 7 or a collecting device. The problems that in the prior art, only one reactor is arranged in one heating furnace, so that the reaction is insufficient, the reaction rate is low, the yield and the purity of the product are high and the like are solved, and the reaction can be fully performed by arranging the continuous heating furnace 5 and the reactor 6, so that the reaction rate is effectively improved, and the yield and the purity of the product are improved.
In another embodiment, holes are formed in the tube plates 4-6 of the wound tube type heat exchanger 4 and are arranged in a regular triangle shape, the high-temperature ends (the high-temperature ends are close to the tube pass outlet) of the tube plates 4-6 are connected with the heat exchange tubes 4-8 of the wound tube type heat exchanger 4 through deep hole welding, and the heat exchange tubes 4-8 are communicated with the holes in the tube plates 4-6. The tube plates 4-6 adopt regular triangle tube arrangement, the maximum number of tubes can be arranged on the same tube plate area in a regular triangle arrangement form (as shown in figure 4), the arrangement is compact, and tube pass fluid directly scours the heat exchange tubes 4-8, so that the tube pass fluid is distributed more uniformly; carbon ions are easily accumulated at the high-temperature end of the tube plate, and the heat exchange tube is broken, so that deep hole welding is adopted, firm connection is realized, and the problems of cracking and breaking are effectively solved. The hole interval on the tube sheet is 22mm, and the interval of adoption is little, can the many cloth pipes, reduces the panel size.
Example 1
A propane dehydrogenation process comprises the following specific steps:
the raw material (propane) in the raw material storage tank 1 flows through a raw material cooler 2, is cooled to minus 87 ℃, then flows through a cold feed heat exchanger 3 to exchange heat and raise the temperature to 45 ℃, enters a wound tube type heat exchanger 4, is heated to 550 ℃ through heat exchange of reaction products, continues flowing, enters a first reactor 6-1 after being heated to 620 ℃ through a first heating furnace 5-1, is subjected to dehydrogenation reaction, and then is reacted to obtain a reaction product at 550 ℃; the reaction product continuously flows, is heated to 625 ℃ by a second heating furnace 5-2 and then enters a second reactor 6-2 for dehydrogenation reaction, and the reaction product cooled to 571 ℃ is obtained after the reaction; the reaction product continuously flows, is heated to 625 ℃ by a third heating furnace 5-3 and then enters a third reactor 6-3 for dehydrogenation reaction, and the reaction product cooled to 577 ℃ is obtained after the reaction; the reaction product continuously flows into the shell side of the wound tube type heat exchanger 4, and the final product with the temperature of 140 ℃ is obtained after heat exchange with the raw material, and flows out of the shell side of the wound tube type heat exchanger 4 to flow into a subsequent treatment system.
According to the propane dehydrogenation process, the winding tube type heat exchanger is selected, the heat exchange effect is good, the load of a subsequent heating furnace is reduced, meanwhile, the reaction raw material is heated by utilizing the waste heat of the reaction product, more than 1000 ten thousand yuan of fuel can be saved each year, heat can be provided for the raw material, the waste heat of the reaction product is effectively recycled, the temperature of the reaction product is effectively reduced, the problem that the reaction raw material needs high energy consumption for heating is solved, and the problem that the temperature of the product is high and the cooling load is large is solved; after the original floating head heat exchanger is replaced by a wound tube heat exchanger, the tube shell process materials are exchanged, so that the process requirements can be met; through the system, the cost of propane dehydrogenation is effectively reduced, and the production efficiency is improved.
Claims (10)
1. A propane dehydrogenation process is characterized in that the process of temperature rise firstly utilizes the waste heat of a reaction product to exchange heat with raw materials in a wound tube type heat exchanger (4), then the raw materials are heated in a heating furnace (5), and then the raw materials enter the reactor (6) for reaction.
2. The propane dehydrogenation process according to claim 1, wherein the raw material is subjected to heat exchange in a wound tube heat exchanger (4), heated by a heating furnace (5), and then enters a reactor (6) for reaction, the obtained reaction product is heated by another heating furnace (5), and then enters another reactor (6) for reaction, the obtained reaction product is heated by the next heating furnace (5), and then enters another reactor (6) for reaction, and the obtained reaction product is subjected to heat exchange with the raw material in the wound tube heat exchanger (4) and then is converged into a subsequent treatment system.
3. The propane dehydrogenation process according to claim 1, wherein the raw material is cooled and then heated, and finally enters the wound tube heat exchanger (4) to exchange heat with the reaction product.
4. The propane dehydrogenation process according to claim 1, wherein the propane dehydrogenation system comprises a raw material storage tank (1), a wound tube heat exchanger (4), a reactor (6) and a heating furnace (5); the raw material storage tank (1) is sequentially connected with a raw material cooler (2), a cold feeding heat exchanger (3), a tube side of a wound tube type heat exchanger (4), a heating furnace (5), a reactor (6), a shell side of the wound tube type heat exchanger (4) and a subsequent treatment system (7).
5. A propane dehydrogenation process according to claim 4, characterized in that a feed cooler (2) and a cold feed heat exchanger (3) are arranged between the feed storage tank (1) and the wound tube heat exchanger (4).
6. A propane dehydrogenation process according to claim 4, wherein the reactor (6) comprises a first reactor (6-1), a second reactor (6-2) and a third reactor (6-3), and the furnace (5) comprises a first furnace (5-1), a second furnace (5-2) and a third furnace (5-3); the tube side outlet (4-1) of the winding tube type heat exchanger (4) is sequentially connected with a first heating furnace (5-1), a first reactor (6-1), a second heating furnace (5-2), a second reactor (6-2), a third heating furnace (5-3), a third reactor (6-3) and a shell side inlet (4-4) of the heat exchanger.
7. A propane dehydrogenation process according to claim 4, wherein holes are arranged on the tube plates (4-6) of the wound tube heat exchanger (4), the holes are arranged in a regular triangle, the high-temperature ends of the tube plates (4-6), the tube plates (4-6) are connected with the heat exchange tubes (4-8) of the wound tube heat exchanger (4) by deep hole welding, and the heat exchange tubes (4-8) are communicated with the holes on the tube plates (4-6).
8. A propane dehydrogenation process according to claim 7, wherein the tube sheets (4-6) have a hole pitch of 22mm.
9. The propane dehydrogenation process according to claim 4, wherein flushing pipes (4-7) are respectively wound above and below the outer side of the shell of the wound pipe type heat exchanger (4), openings A are uniformly arranged on the flushing pipes (4-7), an opening B is arranged at the position, corresponding to the opening A, of the shell of the wound pipe type heat exchanger, the opening A on the flushing pipe (4-7) is connected with the opening B on the shell, the flushing pipes (4-7) are connected with a flushing pipeline, and a valve is arranged on the flushing pipeline; openings C (4-5) are arranged on a tube side outlet (4-1) and a tube side inlet (4-2), a shell side outlet (4-3) and a shell side inlet (4-4) of the winding tube type heat exchanger (4), the openings C (4-5) are connected with a flushing pipeline, and a valve is arranged on the flushing pipeline.
10. Propane dehydrogenation system according to claim 4, characterized in that impingement plates (4-9) are provided at the shell inlet (4-4) of the wound tube heat exchanger (4).
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211333107.9A CN115894145A (en) | 2022-10-28 | 2022-10-28 | Propane dehydrogenation process |
| PCT/CN2022/142197 WO2023197683A1 (en) | 2022-10-28 | 2022-12-27 | Propane dehydrogenation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211333107.9A CN115894145A (en) | 2022-10-28 | 2022-10-28 | Propane dehydrogenation process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115894145A true CN115894145A (en) | 2023-04-04 |
Family
ID=86490387
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211333107.9A Pending CN115894145A (en) | 2022-10-28 | 2022-10-28 | Propane dehydrogenation process |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN115894145A (en) |
| WO (1) | WO2023197683A1 (en) |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL113071C (en) * | 1961-06-12 | |||
| ES2254555T5 (en) * | 2002-05-27 | 2013-02-15 | Air Products And Chemicals, Inc. | Heat exchanger with tube coils |
| DK2454546T3 (en) * | 2009-07-16 | 2015-10-05 | Lockheed Corp | Spiral rørbundtsarrangementer for heat exchangers |
| CN208098029U (en) * | 2018-02-13 | 2018-11-16 | 镇海石化建安工程有限公司 | Dehydrogenating propane device |
| CN108160006B (en) * | 2018-02-13 | 2023-11-14 | 镇海石化建安工程股份有限公司 | Propane dehydrogenation device and propane dehydrogenation method |
| CN213977483U (en) * | 2020-11-13 | 2021-08-17 | 洛阳智达石化工程有限公司 | System for light hydrocarbon modification and propane dehydrogenation jointly produce propylene |
-
2022
- 2022-10-28 CN CN202211333107.9A patent/CN115894145A/en active Pending
- 2022-12-27 WO PCT/CN2022/142197 patent/WO2023197683A1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| WO2023197683A1 (en) | 2023-10-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2016045585A1 (en) | Large reactor and device and process thereof | |
| CN105032305B (en) | A kind of new radial direction plate-type reactor | |
| US8071059B2 (en) | Chemical reactor | |
| CN218689323U (en) | Propane dehydrogenation system | |
| WO2024066519A1 (en) | Heat exchange assembly for hydrogenation device, and heat exchange process | |
| CN115894145A (en) | Propane dehydrogenation process | |
| CN101380561B (en) | Large membrane wall gas-phase reactor with high pressure steam as by-product | |
| CN103585933A (en) | Corrugated board type uniform-temperature hydrogenation reactor | |
| CN105776141A (en) | Novel fixed bed reactor for preparing chlorine gas through catalytic oxidation of hydrogen chloride | |
| CN115523774A (en) | Heat recovery system for heat high-pressure gas in hydrogenation device | |
| CN104248939B (en) | Methanol oxidizer in silver catalyst process formaldehyde device | |
| CN209854079U (en) | Optimization device of hydrocracking heat exchange technology | |
| CN209968376U (en) | But epoxypropane synthesizer of continuous regeneration catalyst | |
| CN209043115U (en) | It is a kind of can on-line cleaning input and output material heat exchanger | |
| CN205919713U (en) | Novel heat transfer system of no tube sheet methanol oxidation ware | |
| CN219200136U (en) | Square spiral plate type heat exchanger | |
| CN204159316U (en) | Methanol oxidation device in a kind of silver-colored formaldehyde device | |
| CN102072679B (en) | L-shaped tube heat exchanger | |
| CN104230616B (en) | Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system | |
| CN215893343U (en) | Combined double-shell-pass U-shaped tubular heat exchanger | |
| CN218673259U (en) | Energy-saving corrosion-resistant heat exchange device | |
| CN220432742U (en) | Soybean plate type tempering tower | |
| CN220803143U (en) | Tube type fixed bed reactor | |
| CN219037695U (en) | Coiled pipe heat exchange device, continuous reforming process system and hydrogenation heat exchange process system thereof | |
| CN216011866U (en) | Combined double-shell-pass continuous spiral baffle plate type heat exchanger |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |