Method and device for efficiently converting light hydrocarbon to increase additional value

Abstract

The invention relates to the technical field of light hydrocarbon conversion, in particular to a method and a device for efficiently converting light hydrocarbon to increase additional value, and the method comprises the following steps: reacting the raw material light hydrocarbon through a supergravity reactor filled with a catalyst and a second reactor, and condensing and separating the reaction product to obtain a gas-phase component rich in propane and a liquid-phase component rich in aromatic hydrocarbon. According to the method, light hydrocarbon with low additional value is subjected to isomerization, catalytic cracking, aromatization, hydrogen transfer and other reactions, and a liquid-phase product rich in aromatic hydrocarbon and a propane gas-phase product with high selectivity are obtained. The method disclosed by the invention is simple in reaction process and short in flow, the product is rich in aromatic hydrocarbon and propane at the same time, the additional value of light hydrocarbon is improved, and high-valued utilization of low-weight light hydrocarbon resources is realized.

Description

Technical Field

[0001] The invention relates to the technical field of light hydrocarbon conversion, and is a method and device for efficiently converting light hydrocarbons to increase added value. Background Art

[0002] C5, C6 light hydrocarbons, as well as topped oil, raffinate, reformate and other refinery by-products have a wide range of sources, low aromatic potential, high saturated vapor pressure, and low octane number (RON is 60 to 70), making them unsuitable for use as blending components of high-grade gasoline and aromatic reforming raw materials. How to effectively utilize the considerable amount of light alkane resources and increase their added value has become an urgent problem for petrochemical companies to solve.

[0003] Aromatics are important basic raw materials for the chemical industry. The conversion of light hydrocarbons into aromatics and other chemical products is bound to be the first choice of chemical companies, especially paraxylene (PX) in light aromatics BTX (benzene, toluene, xylene, etc.), which is mainly used to produce terephthalic acid (PTA), and then used to produce polyester products such as polyethylene terephthalate (PET). It is widely used in chemical fibers, light industry, electronics, construction and other fields, and is closely related to the level of people's living standards.

[0004] Propylene, the product of propane dehydrogenation, is an important petrochemical intermediate, second only to ethylene in importance. It is widely used in the production of organic raw materials such as polypropylene, butanol, octanol, acrylonitrile, acrylic acid, propylene oxide, isopropyl benzene and isopropyl acid, and has good prospects.

[0005] Based on the above analysis, refineries produce a large amount of low-quality light hydrocarbon resources as by-products, and aromatics and propane resources are in urgent need of developing a method for efficient conversion of light hydrocarbons to increase added value, thereby obtaining products rich in aromatics and propane.

[0006] A Chinese patent document with publication number CN101314731B discloses a method for non-hydrogen aromatization of light hydrocarbons, comprising the following steps: mixing naphtha and C3 to C5 light hydrocarbons and then entering a moving bed reaction zone, contacting with an aromatization catalyst to carry out an aromatization reaction, and the spent catalyst flowing out from the bottom of the moving bed reaction zone passes through a spent catalyst lifter, a spent catalyst lift pipeline, a spent catalyst separation hopper and a pressure conversion and flow control zone to enter a catalyst regenerator from the top, and passes through a buffer zone, a charring zone, a drying zone and a cooling zone in the catalyst regenerator from top to bottom in sequence, and oxygen-containing regeneration gas is introduced into the charring zone to carry out charring regeneration of the spent catalyst, and then the regenerated catalyst is lifted and enters the moving bed reactor from the top.

[0007] This method can convert low-octane naphtha and low-carbon hydrocarbons into high-octane gasoline components and high-quality liquefied gas using a moving bed, but the operation is relatively complicated, the process flow is relatively long, the aromatics selectivity is low (<35%), and it is not rich in propane. In other words, the existing light hydrocarbon conversion and utilization processes are mostly used to produce aromatics, gasoline or olefins, and cannot take all three into account. There are problems such as low carbon-based conversion rate of raw materials, low added value of products and high energy consumption of production equipment. Summary of the invention

[0008] The present invention provides a method and device for efficiently converting light hydrocarbons to increase added value, which overcomes the deficiencies of the above-mentioned prior art and can effectively solve the problems of low raw material conversion rate and low product added value in the existing light hydrocarbon conversion and utilization process.

[0009] One of the technical solutions of the present invention is achieved by the following measures: A method for efficiently converting light hydrocarbons to increase added value is carried out according to the following steps: S1, preheating the required amount of light hydrocarbons and sending them into the first reactor filled with catalyst 1 for reaction; S2, sending the reaction product obtained in S1 to a second reactor filled with catalyst 2 for reaction; S3, condensing and separating the reaction product obtained in S2 to obtain a propane-rich gas phase component and an aromatics-rich liquid phase component.

[0010] The following is a further optimization and / or improvement of one of the above-mentioned technical solutions: The light hydrocarbon is one of monomer hydrocarbons or mixed oils, the monomer hydrocarbon is one of butane, pentane and hexane, and the mixed oil is one of aromatic raffinate oil, reforming top oil, hydrocracking naphtha and pentane oil.

[0011] The raw materials of the above-mentioned catalyst one and catalyst two include 40 to 90 parts of active components, 20 to 60 parts of binders, 0.5 to 5.0 parts of peptizers and 3 to 15 parts of water in parts by weight, and are obtained by the following steps: the required amount of active components and binders are mixed, and then the required amount of peptizers and water are added to knead and extrude into strips, and the formed solid is dried and calcined to obtain; wherein, the drying temperature is 120°C to 150°C, the drying time is 6h to 12h, the calcination temperature is 500°C to 650°C, and the calcination time is 12h to 24h.

[0012] The active components of the above catalysts 1 and 2 are both high-silicon five-membered ring zeolite, high-silicon five-membered ring zeolite modified with zinc or high-silicon five-membered ring zeolite modified with group VA elements.

[0013] The high silicon five-membered ring type zeolite is ZSM-5 molecular sieve, ZSM-11 molecular sieve or ZSM-12 molecular sieve.

[0014] The molar ratio of silicon oxide to aluminum oxide in the high-silicon five-membered ring type zeolite is 10 to 300.

[0015] The molar ratio of silicon oxide to aluminum oxide in the high-silicon five-membered ring type zeolite is 30 to 150.

[0016] The mass percentage of zinc in the zinc-modified high-silicon five-membered ring zeolite is 0.5% to 3.0%, and the zinc is selected from one or more of zinc chloride, zinc sulfate or zinc nitrate.

[0017] The VA group element in the high silicon five-membered ring zeolite modified with the VA group element is phosphorus, and the mass percentage of phosphorus in the high silicon five-membered ring zeolite containing the VA group element is 0.1% to 2.0%, and the phosphorus is selected from one or more of phosphoric acid, phosphotungstic acid or ammonium phosphomolybdic acid.

[0018] The binder is one or more of pseudo-boehmite, boehmite and silica sol.

[0019] The peptizing agent is one or more of nitric acid, hydrochloric acid, acetic acid and formic acid.

[0020] In the above step S1, the preheating temperature is 50°C to 200°C, and in step S3, the condensing temperature is 0°C to 15°C.

[0021] In the above steps S1 and S2, the reaction pressure is 0 MPa to 3 MPa, the reaction temperature is 300°C to 600°C, and the mass space velocity of light hydrocarbons is 0.1 h -1 Up to 5.0h -1 .

[0022] The first reactor is a supergravity reactor, and the supergravity level of the supergravity reactor is 5g to 400g.

[0023] The second technical solution of the present invention is achieved through the following measures: a device for implementing a method for efficiently converting light hydrocarbons to increase added value, comprising a light hydrocarbon tank, a preheater, a supergravity reactor, a second reactor, a condenser, a gas-liquid separation tank and a liquid product tank, a first processing pipeline fixedly connected between the outlet of the light hydrocarbon tank and the inlet of the preheater, a metering pump fixedly installed on the first processing pipeline, a second processing pipeline fixedly connected between the outlet of the preheater and the raw material inlet of the supergravity reactor, a carrier gas inlet pipeline fixedly connected to the carrier gas inlet of the supergravity reactor, a third processing pipeline fixedly connected between the outlet of the supergravity reactor and the inlet of the second reactor, a fourth processing pipeline fixedly connected between the outlet of the second reactor and the inlet of the condenser, a fifth processing pipeline fixedly connected between the outlet of the condenser and the inlet of the gas-liquid separation tank, a gas phase product delivery pipeline fixedly connected to the gas phase outlet of the gas-liquid separation tank, and a liquid phase product delivery pipeline fixedly connected between the liquid phase outlet of the gas-liquid separation tank and the inlet of the liquid phase product tank.

[0024] The present invention allows low value-added light hydrocarbons to react in a supergravity reactor and a second reactor equipped with a catalyst, and reactions such as isomerization, catalytic cracking, aromatization and hydrogen transfer occur to obtain a liquid phase product rich in aromatics and a highly selective propane gas phase product. The present invention has a simple reaction process and a short flow, and the product is rich in aromatics while taking propane into account, thereby increasing the added value of light hydrocarbons and realizing the high-value utilization of low-quality light hydrocarbon resources. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Attached Figure 1 This is a schematic diagram of the process flow of the optimal embodiment 28 of the present invention.

[0026] The codes in the accompanying drawings are: 1 is a light hydrocarbon tank, 2 is a metering pump, 3 is a preheater, 4 is an ultra-gravity reactor, 5 is a second reactor, 6 is a condenser, 7 is a gas-liquid separation tank, 8 is a liquid product tank, 9 is a gas product delivery pipeline, 10 is a carrier gas inlet pipeline, 11 is a first processing pipeline, 12 is a second processing pipeline, 13 is a third processing pipeline, 14 is a fourth processing pipeline, 15 is a fifth processing pipeline, and 16 is a liquid product delivery pipeline. DETAILED DESCRIPTION

[0027] The present invention is not limited by the following embodiments, and specific implementation methods can be determined according to the technical scheme of the present invention and actual conditions. Unless otherwise specified, the various chemical reagents and chemicals mentioned in the present invention are all chemical reagents and chemicals known and used in the prior art; unless otherwise specified, the percentages in the present invention are all mass percentages; unless otherwise specified, the solutions in the present invention are all aqueous solutions in which the solvent is water, for example, the hydrochloric acid solution is an aqueous hydrochloric acid solution.

[0028] The present invention will be further described below in conjunction with embodiments: Example 1: Figure 1 As shown, the method for efficiently converting light hydrocarbons to increase added value is carried out according to the following steps: S1, the required amount of light hydrocarbons is preheated and sent into the first reactor 4 filled with catalyst 1 for reaction; S2, sending the reaction product obtained in S1 to a second reactor 5 filled with catalyst 2 for reaction; S3, condensing and separating the reaction product obtained in S2 to obtain a propane-rich gas phase component and an aromatics-rich liquid phase component.

[0029] The method for efficiently converting light hydrocarbons to increase added value of the present invention is a non-hydrogenation condition.

[0030] Example 2: As an optimization of the above example, the light hydrocarbon is one of monomer hydrocarbons or mixed oils, the monomer hydrocarbon is one of butane, pentane and hexane, and the mixed oil is one of aromatic raffinate oil, reforming top oil, hydrocracking naphtha and pentane oil.

[0031] Example 3: As an optimization of the above example, the raw materials of Catalyst 1 and Catalyst 2 include 40 to 90 parts of active components, 20 to 60 parts of binder, 0.5 to 5.0 parts of peptizing agent and 3 to 15 parts of water in parts by weight, and are obtained by the following steps: the required amount of active components and binder are mixed, and then the required amount of peptizing agent and water are added to knead and extrude into strips, and the formed solid is dried and calcined; wherein the drying temperature is 120°C to 150°C, the drying time is 6h to 12h, the calcination temperature is 500°C to 650°C, and the calcination time is 12h to 24h.

[0032] Example 4: As an optimization of the above example, the active components of Catalyst 1 and Catalyst 2 are both high-silicon five-membered ring zeolite, high-silicon five-membered ring zeolite modified with zinc or high-silicon five-membered ring zeolite modified with group VA elements.

[0033] Example 5: As an optimization of the above example, the high silicon five-membered ring type zeolite is ZSM-5 molecular sieve, ZSM-11 molecular sieve or ZSM-12 molecular sieve.

[0034] Example 6: As an optimization of the above example, the molar ratio of silicon oxide to aluminum oxide in the high silicon five-membered ring type zeolite is 10 to 300.

[0035] Example 7: As an optimization of the above example, the molar ratio of silicon oxide to aluminum oxide in the high silicon five-membered ring type zeolite is 30 to 150.

[0036] Example 8: As an optimization of the above example, the mass percentage of zinc in the zinc-modified high-silicon five-membered ring zeolite is 0.5% to 3.0%, and zinc is selected from one or more of zinc chloride, zinc sulfate or zinc nitrate.

[0037] Example 9: As an optimization of the above example, the VA group element in the high silicon five-membered ring zeolite modified with the VA group element is phosphorus, and the mass percentage of phosphorus in the high silicon five-membered ring zeolite containing the VA group element is 0.1% to 2.0%, and the phosphorus is selected from one or more of phosphoric acid, phosphotungstic acid or ammonium phosphomolybdic acid.

[0038] In Example 8 and Implementation 9 of the present invention, the modification is carried out by the existing equal volume impregnation method and ion exchange method without limitation.

[0039] Embodiment 10: As an optimization of the above embodiment, the binder is one or more of pseudo-boehmite, boehmite and silica sol.

[0040] Embodiment 11: As an optimization of the above embodiment, the peptizing agent is one or more of nitric acid, hydrochloric acid, acetic acid and formic acid.

[0041] Embodiment 12: As an optimization of the above embodiment, in step S1, the preheating temperature is 50°C to 200°C, and in step S3, the condensation temperature is 0°C to 15°C.

[0042] Example 13: As an optimization of the above example, in steps S1 and S2, the reaction pressure is 0 MPa to 3 MPa, the reaction temperature is 300°C to 600°C, and the mass space velocity of light hydrocarbons is 0.1 h -1 Up to 5.0h -1 .

[0043] Embodiment 14: As an optimization of the above embodiment, the first reactor 4 is a supergravity reactor, and the supergravity level of the supergravity reactor is 5g to 400g.

[0044] In the present invention, the first reactor 4 is a supergravity reactor, and the specific type of the supergravity reactor is not limited; the supergravity level of the supergravity reactor is determined by the magnitude of the centrifugal force generated by the rotation of the supergravity reactor rotor, that is, different supergravity levels can be obtained by adjusting the speed of the rotor by adjusting the motor.

[0045] In the present invention, the type of the second reactor 5 is not limited, and the second reactor 5 can be a fixed bed, a moving bed or a fluidized bed reactor, preferably a fixed bed reactor.

[0046] The present invention utilizes a supergravity reactor to efficiently convert light hydrocarbons to aromatics and propane, making full use of the supergravity environment to improve the mass transfer efficiency between the reaction materials and the catalyst during the reaction. At the same time, the present invention obtains high-content aromatics and propane through specific catalysts, suitable supergravity levels, reaction temperatures, reaction pressures and mass space velocity.

[0047] Embodiment 15: The method for efficiently converting light hydrocarbons to increase added value is carried out according to the following steps: S1, preheat the required amount of butane to 50℃ and send it into the supergravity reactor filled with catalyst 1 for reaction; wherein the reaction pressure is 0MPa, the reaction temperature is 300℃, and the mass space velocity of light hydrocarbon is 0.1h -1 ; The hypergravity level of the hypergravity reactor is 5g; S2, the reaction product obtained in S1 is sent to the second reactor 5 filled with catalyst 2 for reaction; wherein the reaction pressure is 0MPa, the reaction temperature is 300°C, and the mass space velocity of light hydrocarbons is 0.1h -1 ; S3, condensing the reaction product obtained in S2 to 0°C, and then performing gas-liquid separation to obtain a propane-rich gas phase component and an aromatics-rich liquid phase component; The raw materials of catalyst 1 include, by weight, 40 parts of active component (ZSM-5 molecular sieve (SiO2 / Al2O3=10), 20 parts of binder (pseudo-boehmite), 0.5 parts of peptizing agent (nitric acid) and 3 parts of water; The raw materials of catalyst 2 include 40 parts of active component ZSM-5 molecular sieve (SiO2 / Al2O3=300), 20 parts of binder (pseudo-boehmite), 0.5 parts of peptizing agent (nitric acid) and 3 parts of water by weight; Catalyst 1 and Catalyst 2 are both obtained by the following steps: the required amount of active components and binder are mixed, and then the required amount of peptizer and water are added to knead and extrude into strips, and the formed solid is dried and calcined; wherein the drying temperature is 120°C, the drying time is 6h, the calcination temperature is 500°C, and the calcination time is 12h.

[0048] Embodiment 16: The method for efficiently converting light hydrocarbons to increase added value is carried out according to the following steps: S1, preheat the required amount of aromatic raffinate oil to 200℃ and send it into a supergravity reactor filled with catalyst 1 for reaction; wherein the reaction pressure is 3MPa, the reaction temperature is 600℃, and the mass space velocity of light hydrocarbons is 5.0h -1 ; The hypergravity level of the hypergravity reactor is 400g; S2, the reaction product obtained in S1 is sent to the second reactor 5 filled with catalyst 2 for reaction; wherein the reaction pressure is 3MPa, the reaction temperature is 600℃, and the mass space velocity of light hydrocarbons is 5.0h -1 ; S3, condensing the reaction product obtained in S2 to 15° C., and then performing gas-liquid separation to obtain a propane-rich gas phase component and an aromatics-rich liquid phase component; The raw materials of catalyst 1 include, by weight, 90 parts of active component zinc chloride-modified ZSM-11 molecular sieve (SiO2 / Al2O3=30, loaded zinc 3.0%), 60 parts of binder (boehmite), 5.0 parts of peptizing agent (hydrochloric acid) and 15 parts of water; The raw materials of catalyst 2 include, by weight, 90 parts of active component zinc chloride-modified ZSM-11 molecular sieve (SiO2 / Al2O3=150, loaded zinc 3.0%), 60 parts of binder (boehmite), 5.0 parts of peptizing agent (hydrochloric acid) and 15 parts of water; Catalyst 1 and Catalyst 2 are both obtained by the following steps: the required amount of active components and binder are mixed, and then the required amount of peptizer and water are added to knead and extrude into strips, and the formed solid is dried and calcined; wherein the drying temperature is 150°C, the drying time is 12h, the calcination temperature is 650°C, and the calcination time is 24h.

[0049] Embodiment 17: The method for efficiently converting light hydrocarbons to increase added value is carried out according to the following steps: S1, preheat the required amount of pentane oil to 100 ° C, and send it into the supergravity reactor filled with catalyst 1 for reaction; wherein the reaction pressure is 1.5 MPa, the reaction temperature is 450 ° C, and the mass space velocity of light hydrocarbons is 3.0 h -1 ; The hypergravity level of the hypergravity reactor is 200g; S2, the reaction product obtained in S1 is sent to the second reactor 5 filled with catalyst 2 for reaction; wherein the reaction pressure is 1.5MPa, the reaction temperature is 450℃, and the mass space velocity of light hydrocarbons is 3.0h -1 ; S3, condensing the reaction product obtained in S2 to 10° C., and then performing gas-liquid separation to obtain a propane-rich gas phase component and an aromatics-rich liquid phase component; The raw materials of catalyst 1 include 60 parts of active component (phosphoric acid-modified ZSM-12 molecular sieve (SiO2 / Al2O3=100, loaded phosphorus 1.0%)), 40 parts of binder (silica sol), 3.0 parts of peptizing agent (acetic acid) and 10 parts of water by weight; The raw materials of catalyst 2 include, by weight, 60 parts of active component (ZSM-12 molecular sieve modified with phosphoric acid (SiO2 / Al2O3=200, loaded phosphorus 1.0%)), 40 parts of binder (boehmite, boehmite and silica sol), 3.0 parts of peptizing agent (nitric acid, hydrochloric acid, acetic acid and formic acid) and 10 parts of water; Catalyst 1 and Catalyst 2 are obtained by the following steps: the required amount of active components and binder are mixed, and then the required amount of peptizer and water are added to knead and extrude into strips, and the formed solid is dried and calcined; wherein the drying temperature is 130°C, the drying time is 9h, the calcination temperature is 600°C, and the calcination time is 20h.

[0050] The present invention allows low value-added raw light hydrocarbons to react in two reactors, namely, an ultra-gravity reactor and a second reactor 5, to undergo aromatization, isomerization, hydrogen transfer, catalytic cracking and other reactions, thereby obtaining highly selective aromatics and a propane-rich gas phase product, with an aromatics yield of 42.5% to 55.2%; the propane selectivity in the gas phase is 30.4% to 45.3%, the reaction is mild and controllable, the process is short, and the operation is simple.

[0051] Embodiment 18: The difference from Example 17 is that in step S1, the light hydrocarbon is aromatic raffinate oil, the supergravity reactor forms a supergravity level of 50g, the reaction temperature is 400°C, the reaction pressure is 0.5MPa (N2), and the mass space velocity of the light hydrocarbon is 0.8h-1 The active ingredient in the catalyst 1 is ZSM-5 molecular sieve (SiO2 / Al2O3=60); in step S2, the reaction temperature is 380°C, the reaction pressure is 0.5MPa (N2), and the mass space velocity of light hydrocarbons is 1.5h -1 The active ingredient in Catalyst 2 is ZSM-5 molecular sieve (SiO2 / Al2O3=60); the remaining steps are the same as Example 17.

[0052] The aromatics content obtained by the method of Example 18 of the present invention is 45.3%, and the propane content is 35.5%.

[0053] Embodiment 19: The difference from Example 17 is that in step S1, the light hydrocarbon is straight-run naphtha, the high-gravity reactor forms a high-gravity level of 100 g, the reaction temperature is 520° C., the reaction pressure is 0 MPa, and the mass space velocity of the light hydrocarbon is 1.2 h -1 The active ingredient in the catalyst 1 is ZSM-5 molecular sieve modified with zinc chloride (SiO2 / Al2O3=150, loaded with 2% zinc); in step S2, the reaction temperature is 450°C, the reaction pressure is 0 MPa, and the mass space velocity of light hydrocarbons is 1.0 h -1 The active ingredient in Catalyst 2 is ZSM-11 molecular sieve (SiO2 / Al2O3=100); the remaining steps are the same as those in Example 17.

[0054] The aromatics content obtained by the method of Example 19 of the present invention is 46.7%, and the propane content is 30.4%.

[0055] Embodiment 20: The difference from Example 17 is that in step S1, the light hydrocarbon is aromatic raffinate oil, the supergravity reactor forms a supergravity level of 5g, the reaction temperature is 390°C, the reaction pressure is 0.1MPa (N2), and the mass space velocity of the light hydrocarbon is 1.0h -1 The active ingredient in the catalyst 1 is ZSM-12 molecular sieve (SiO2 / Al2O3=150); in step S2, the reaction temperature is 400°C, the reaction pressure is 0.1MPa (N2), and the mass space velocity of light hydrocarbons is 0.5h -1 The active ingredient in Catalyst 2 is ZSM-5 molecular sieve modified with phosphoric acid (SiO2 / Al2O3=240, loaded phosphorus 0.5%); the remaining steps are the same as those in Example 17.

[0056] The aromatics content obtained by the method of Example 20 of the present invention is 42.5%, and the propane content is 32.4%.

[0057] Embodiment 21: The difference from Example 17 is that in step S1, the light hydrocarbon is reformed top oil, the high gravity reactor forms a high gravity level of 200g, the reaction temperature is 400°C, the reaction pressure is 1.0MPa (N2), and the mass space velocity of the light hydrocarbon is 0.5h -1 The active ingredient in the catalyst 1 is ZSM-5 molecular sieve modified with zinc nitrate (SiO2 / Al2O3=30, loaded with 2% zinc); in step S2, the reaction temperature is 350°C, the reaction pressure is 1.0MPa (N2), and the mass space velocity of light hydrocarbons is 0.5h -1 The active ingredient in Catalyst 2 is ZSM-5 molecular sieve modified with zinc nitrate (SiO2 / Al2O3=270, loaded zinc 2%); the remaining steps are the same as those in Example 17.

[0058] The aromatics content obtained by the method of Example 21 of the present invention is 46.6%, and the propane content is 34.6%.

[0059] Embodiment 22: The difference from Example 17 is that in step S1, the light hydrocarbon is reformed top oil, the high gravity reactor forms a high gravity level of 150g, the reaction temperature is 300°C, the reaction pressure is 0MPa, and the mass space velocity of the light hydrocarbon is 0.5h -1 The active ingredient in the catalyst 1 is ZSM-11 molecular sieve (SiO2 / Al2O3=300); in step S2, the reaction temperature is 440°C, the reaction pressure is 0MPa, and the mass space velocity of light hydrocarbons is 1.5h -1 The active ingredient in Catalyst 2 is ZSM-12 molecular sieve (SiO2 / Al2O3=90); the remaining steps are the same as those in Example 17.

[0060] The aromatics content obtained by the method of Example 22 of the present invention is 54.6%, and the propane content is 42.1%.

[0061] Embodiment 23: The difference from Example 17 is that in step S1, the light hydrocarbon is reformed tops oil, the high gravity reactor forms a high gravity level of 180g, the reaction temperature is 450°C, the reaction pressure is 0MPa, and the mass space velocity of the light hydrocarbon is 1.5h -1 The active ingredient in the catalyst 1 is ZSM-5 molecular sieve modified with phosphoric acid and zinc nitrate (SiO2 / Al2O3=180, loaded with 1% phosphorus and 2% zinc); in step S2, the reaction temperature is 450°C, the reaction pressure is 0MPa, and the mass space velocity of light hydrocarbons is 1.5h -1 The active ingredient in Catalyst 2 is ZSM-5 molecular sieve (SiO2 / Al2O3=270); the remaining steps are the same as Example 17.

[0062] The aromatics content obtained by the method of Example 23 of the present invention is 55.2%, and the propane content is 45.3%.

[0063] Embodiment 24: The difference from Example 17 is that in step S1, the light hydrocarbon is n-butane (purity greater than 99%), the high gravity reactor forms a high gravity level of 250g, the reaction temperature is 500°C, the reaction pressure is 0MPa, and the mass space velocity of the light hydrocarbon is 2.0h -1 The active ingredient in the catalyst 1 is ZSM-12 molecular sieve (SiO2 / Al2O3=240); in step S2, the reaction temperature is 600°C, the reaction pressure is 0MPa, and the mass space velocity of light hydrocarbons is 1.0h -1 The active ingredient in Catalyst 2 is ZSM-5 molecular sieve (SiO2 / Al2O3=120); the remaining steps are the same as Example 17.

[0064] The aromatics content obtained by the method of Example 24 of the present invention is 50.1%, and the propane content is 39.5%.

[0065] Embodiment 25: The difference from Example 17 is that in step S1, the light hydrocarbon is pentane oil, the high gravity reactor forms a high gravity level of 60g, the reaction temperature is 460°C, the reaction pressure is 0MPa, and the mass space velocity of the light hydrocarbon is 3.0h -1 The active ingredient in the catalyst 1 is ZSM-11 molecular sieve (SiO2 / Al2O3=60); in step S2, the reaction temperature is 470°C, the reaction pressure is 0MPa, and the mass space velocity of light hydrocarbons is 0.5h -1 The active ingredient in Catalyst 2 is ZSM-5 molecular sieve (SiO2 / Al2O3=120); the remaining steps are the same as Example 17.

[0066] The aromatics content obtained by the method of Example 25 of the present invention is 48.5%, and the propane content is 37.9%.

[0067] Embodiment 26: The difference from Example 17 is that in step S1, the light hydrocarbon is hydrocracked naphtha, the high gravity reactor forms a high gravity level of 400g, the reaction temperature is 600°C, the reaction pressure is 0.1MPa (N2), and the mass space velocity of the light hydrocarbon is 0.5h -1 The active ingredient in the catalyst 1 is ZSM-5 molecular sieve (SiO2 / Al2O3=150); in step S2, the reaction temperature is 450°C, the reaction pressure is 0.1MPa (N2), and the mass space velocity of light hydrocarbons is 0.5h -1The active ingredient in Catalyst 2 is ZSM-11 molecular sieve (SiO2 / Al2O3=240); the remaining steps are the same as Example 17.

[0068] The aromatics content obtained by the method of Example 26 of the present invention is 51.5%, and the propane content is 40.1%.

[0069] Embodiment 27: The difference from Example 17 is that in step S1, the light hydrocarbon is aromatic raffinate oil, the high gravity reactor forms a high gravity level of 180g, the reaction temperature is 420°C, the reaction pressure is 3.0MPa (N2), and the mass space velocity of the light hydrocarbon is 1.0h -1 The active ingredient in the catalyst 1 is ZSM-5 molecular sieve modified with zinc sulfate (SiO2 / Al2O3=90); in step S2, the reaction temperature is 380°C, the reaction pressure is 3.0MPa (N2), and the mass space velocity of light hydrocarbons is 2.0h -1 The active ingredient in Catalyst 2 is ZSM-11 molecular sieve modified with phosphotungstic acid (SiO2 / Al2O3=120); the remaining steps are the same as those in Example 17.

[0070] The aromatics content obtained by the method of Example 27 of the present invention is 52.1%, and the propane content is 43.9%.

[0071] Example 28: As shown in the attached Figure 1 As shown, an apparatus for implementing a method for efficiently converting light hydrocarbons to increase added value comprises a light hydrocarbon tank 1, a preheater 3, a first reactor 4, a second reactor 5, a condenser 6, a gas-liquid separation tank 7 and a liquid product tank 8. A first processing pipeline 11 is fixedly connected between the outlet of the light hydrocarbon tank 1 and the inlet of the preheater 3, a metering pump 2 is fixedly installed on the first processing pipeline 11, a second processing pipeline 12 is fixedly connected between the outlet of the preheater 3 and the raw material inlet of the first reactor 4, a carrier gas inlet pipeline 10 is fixedly connected to the carrier gas inlet of the first reactor 4, a third processing pipeline 13 is fixedly connected between the outlet of the first reactor 4 and the inlet of the second reactor 5, a fourth processing pipeline 14 is fixedly connected between the outlet of the second reactor 5 and the inlet of the condenser 6, a fifth processing pipeline 15 is fixedly connected between the outlet of the condenser 6 and the inlet of the gas-liquid separation tank 7, a gas phase product delivery pipeline 9 is fixedly connected to the gas phase outlet of the gas-liquid separation tank, and a liquid phase product delivery pipeline 16 is fixedly connected between the liquid phase outlet of the gas-liquid separation tank 7 and the inlet of the liquid product tank 8.

[0072] In the device for implementing the method for efficiently converting light hydrocarbons to increase added value of the present invention, the feed port of the first reactor 4 includes a raw material inlet and a carrier gas inlet. The raw material inlet feeds light hydrocarbon raw materials, and the carrier gas inlet feeds nitrogen. The nitrogen is used for pressure testing and leak detection to ensure the reaction pressure. As needed, the first reactor 4 is an ultra-gravity reactor.

[0073] The device of the present invention implements the method for efficiently converting light hydrocarbons to increase added value. During use, light hydrocarbons are sent to a preheater 3 by a metering pump 2 for preheating, and the light hydrocarbons preheated to a certain temperature are introduced into a first reactor 4 equipped with a catalyst to carry out a catalytic reaction under the action of supergravity. After the reaction is completed, the obtained intermediate product is further introduced into a second reactor 5 equipped with a catalyst for further reaction, and the obtained final product is sent to a condenser 6 for condensation. The condensed final product is sent to a gas-liquid separation tank 7 for gas-liquid separation, and the separated gas phase product with a high propane content is sent to a subsequent process via a gas phase product delivery pipeline 9, and the separated liquid phase product with a high aromatic content is sent to a liquid phase product tank 8 for temporary storage.

[0074] In summary, the present invention reacts low value-added light hydrocarbons through a supergravity reactor and a second reactor to obtain a liquid phase product rich in aromatics and a highly selective propane gas phase product. The present invention has a simple reaction process and a short flow process. The product is rich in aromatics while taking into account propane, thereby increasing the added value of light hydrocarbons and realizing the high-value utilization of low-quality light hydrocarbon resources.

[0075] The above technical features constitute the embodiments of the present invention, which have strong adaptability and implementation effect. Non-essential technical features can be added or reduced according to actual needs to meet the requirements of different situations.

Claims

1. A method for efficiently converting light hydrocarbons to increase added value, characterized in that Follow these steps: S1, preheating the required amount of light hydrocarbons and sending them into the first reactor filled with catalyst 1 for reaction; S2, sending the reaction product obtained in S1 to a second reactor filled with catalyst 2 for reaction; S3, condensing and separating the reaction product obtained in S2 to obtain a propane-rich gas phase component and an aromatics-rich liquid phase component.

2. The method for efficiently converting light hydrocarbons to increase added value according to claim 1, characterized in that The light hydrocarbon is one of monomer hydrocarbons or mixed oils, the monomer hydrocarbon is one of butane, pentane and hexane, and the mixed oil is one of aromatic raffinate oil, reforming top oil, hydrocracking naphtha and pentane oil.

3. The method for efficiently converting light hydrocarbons to increase added value according to claim 1 or 2, characterized in that The raw materials of catalyst one and catalyst two include 40 to 90 parts of active components, 20 to 60 parts of binders, 0.5 to 5.0 parts of peptizers and 3 to 15 parts of water in parts by weight, and are obtained by the following steps: the required amount of active components and binders are mixed, and then the required amount of peptizers and water are added to knead and extrude into strips, and the formed solid is dried and calcined to obtain; wherein the drying temperature is 120°C to 150°C, the drying time is 6h to 12h, the calcination temperature is 500°C to 650°C, and the calcination time is 12h to 24h.

4. The method for efficiently converting light hydrocarbons to increase added value according to claim 3, characterized in that The active components of the catalyst 1 and the catalyst 2 are both one of high-silicon five-membered ring zeolite, high-silicon five-membered ring zeolite modified with zinc or high-silicon five-membered ring zeolite modified with group VA elements.

5. The method for efficiently converting light hydrocarbons to increase added value according to claim 4, characterized in that The high-silicon five-membered ring type zeolite is ZSM-5 molecular sieve, ZSM-11 molecular sieve or ZSM-12 molecular sieve; or / and the molar ratio of silicon oxide to aluminum oxide in the high-silicon five-membered ring type zeolite is 10 to 300.

6. The method for efficiently converting light hydrocarbons to increase added value according to claim 4 or 5, characterized in that The mass percentage of zinc in the zinc-modified high-silicon five-membered ring zeolite is 0.5% to 3.0%, and the zinc is selected from at least one of zinc chloride, zinc sulfate or zinc nitrate.

7. The method for efficiently converting light hydrocarbons to increase added value according to claim 4, 5 or 6, characterized in that The group VA element in the high silicon five-membered ring zeolite modified with group VA elements is phosphorus, and the mass percentage of phosphorus in the high silicon five-membered ring zeolite containing group VA elements is 0.1% to 2.0%, and the phosphorus is selected from one or more of phosphoric acid, phosphotungstic acid or ammonium phosphomolybdic acid.

8. The method for efficiently converting light hydrocarbons to increase added value according to any one of claims 3 to 7, characterized in that The binder is one or more of pseudo-boehmite, boehmite and silica sol; or / and the peptizing agent is one or more of nitric acid, hydrochloric acid, acetic acid and formic acid.

9. The method for efficiently converting light hydrocarbons to increase added value according to any one of claims 1 to 7, characterized in that In step S1, the preheating temperature is 50°C to 200°C, and in step S3, the condensation temperature is 0°C to 15°C; or / and, in steps S1 and S2, the reaction pressure is 0MPa to 3MPa, the reaction temperature is 300°C to 600°C, and the mass space velocity of light hydrocarbons is 0.1h -1 Up to 5.0h -1 .

10. A device for implementing the method for efficiently converting light hydrocarbons to increase added value according to any one of claims 1 to 9, characterized in that It includes a light hydrocarbon tank, a preheater, a supergravity reactor, a second reactor, a condenser, a gas-liquid separation tank and a liquid product tank. A first processing pipeline is fixedly connected between the light hydrocarbon tank outlet and the preheater inlet, a metering pump is fixedly installed on the first processing pipeline, a second processing pipeline is fixedly connected between the preheater outlet and the raw material inlet of the supergravity reactor, a carrier gas inlet pipeline is fixedly connected to the carrier gas inlet of the supergravity reactor, a third processing pipeline is fixedly connected between the supergravity reactor outlet and the second reactor inlet, a fourth processing pipeline is fixedly connected between the second reactor outlet and the condenser inlet, a fifth processing pipeline is fixedly connected between the condenser outlet and the gas-liquid separation tank inlet, a gas-phase product delivery pipeline is fixedly connected to the gas phase outlet of the gas-liquid separation tank, and a liquid-phase product delivery pipeline is fixedly connected between the liquid phase outlet of the gas-liquid separation tank and the inlet of the liquid product tank.

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