WO2017181814A1 - Dispositif et procédé de séparation pour catalyseur et hydrocarbure lourd dans un réacteur à combustible en suspension - Google Patents

Dispositif et procédé de séparation pour catalyseur et hydrocarbure lourd dans un réacteur à combustible en suspension Download PDF

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WO2017181814A1
WO2017181814A1 PCT/CN2017/078014 CN2017078014W WO2017181814A1 WO 2017181814 A1 WO2017181814 A1 WO 2017181814A1 CN 2017078014 W CN2017078014 W CN 2017078014W WO 2017181814 A1 WO2017181814 A1 WO 2017181814A1
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catalyst
tank
filtrate
filter medium
valve
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PCT/CN2017/078014
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English (en)
Chinese (zh)
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汪大闪
刘倩倩
李昌元
饶莎莎
宋德臣
詹晓东
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武汉凯迪工程技术研究总院有限公司
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Publication of WO2017181814A1 publication Critical patent/WO2017181814A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
    • B01D35/06—Filters making use of electricity or magnetism
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/006—Separating solid material from the gas/liquid stream by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/34—Apparatus, reactors
    • C10G2/342—Apparatus, reactors with moving solid catalysts

Definitions

  • the invention relates to the technical field of petrochemical industry, in particular to a device and a method for separating catalyst and heavy hydrocarbon in a slurry bed reactor.
  • the method of converting the synthesis gas consisting of CO and H 2 into a hydrocarbon by catalytic action was invented by the German scientists Frans Fischer and Hans Tropsch in 1923, referred to as Fischer-Tropsch synthesis.
  • the basic principle is a process in which CO undergoes heterogeneously catalyzed hydrogenation on a metal catalyst to form a mixture of linear alkane and olefin.
  • the industrial Fischer-Tropsch synthesis reactor types are fixed bed, fluidized bed and slurry bed.
  • the slurry bed reactor is the newly developed technology, and has the following advantages compared with the fixed bed reactor and the fluidized bed reactor: 1.
  • the solid catalyst particles used in the slurry bed reactor are very small in diameter, generally 50 to 300 ⁇ m. As the operating time of the reactor increases, the catalyst particles are gradually broken by collision and abrasion, and the slurry in the reactor is in the slurry. The diameter of the solid particles becomes smaller, and the diameter range is expanded to 1 to 300 ⁇ m, which makes it difficult to separate the solid catalyst from the heavy hydrocarbon in the reactor.
  • the methods for separating the solid catalyst from the slurry in the slurry bed reactor are mainly: gravity sedimentation, differential pressure filtration and magnetic separation. Gravity sedimentation is the use of gravity to cause the solid catalyst particles to automatically sink into the bottom of the separation tank to separate from the slurry.
  • One method is to separate the magnetically strong substances by the magnetic force generated by the high-intensity magnetic field; the other method is to use the high-strength magnetic field magnetization catalyst to make the fine catalyst particles automatic. Aggregate large particles to improve solid-liquid separation.
  • U.S. Patent No. 3,829,478 discloses a relatively typical slurry-bed reactor solid-liquid separation system which extracts a solid catalyst-containing slurry from a slurry in the reactor to a separation tank outside the reactor, and solid catalyst particles in the slurry. Settle to the bottom of the tank under the action of gravity. The solid catalyst particles enriched in the bottom of the tank are recycled to the reactor to continue to participate in the reaction, and the slurry containing no catalyst in the upper portion of the tank is directly taken out, thereby separating the catalyst particles from the liquid product. Since the method only separates the catalyst particles from the liquid product by gravity, the diameter of the solid catalyst particles is small, and it takes a long time to separate the catalyst particles from the liquid product, and even some of the fine particles are directly suspended in the slurry and cannot be settled.
  • Chinese patent CN101959575A describes a continuous separation and discharge apparatus and method for a solid catalyst and liquid product of a Fischer-Tropsch synthesis reaction.
  • the patent installs a flat filter or a cartridge filter at the bottom of the reactor, and separates the solid catalyst in the slurry from the liquid product by the pressure difference between the inside and the outside of the filter.
  • the surface filtration efficiency is changed. Low, at this point the pulse device is activated to perform a backwash filter for removing the solid catalyst adhering to the filter.
  • fine catalyst particles will slowly block the filter pores, causing the filter to fail and having to stop and replace the filter.
  • US Patent No. 7,360,657 discloses a continuous slurry-bed Fischer-Tropsch synthesis reaction solid-liquid separation method in which one or more upright magnetic rods are disposed in a magnetic separator, and the slurry enters the magnetic separator from the middle of the magnetic separator, in the slurry.
  • the magnetic catalyst particles are attracted by the magnetic rod, slide down the magnetic rod due to gravity, and the clear liquid flows out from the top outlet of the magnetic separator, and the slurry containing the catalyst particles is discharged from the bottom of the magnetic separator.
  • Chinese patent CN103846160A discloses a separation method of a slurry bed Fischer-Tropsch synthesis heavy product and a catalyst.
  • the Fischer-Tropsch synthesis heavy product from the slurry bed reactor and the magnetic Fischer-Tropsch synthesis catalyst are degassed and then enter the separator.
  • the catalyst In the middle and lower part, the catalyst is initially settled by gravity, and a concentrated slurry rich in catalyst is obtained in the lower part of the separator and recycled to the slurry bed reactor.
  • the slurry enters the magnetic separation zone in the upper part of the separator; in the magnetic separation zone,
  • the chemical is adsorbed in the magnetic field by the magnetic force.
  • the catalyst adsorbed in the magnetic field reaches the set amount, the magnetic field is removed, the catalyst sinks to the diversion tube by gravity, flows along the diversion tube to the bottom of the separator, and circulates back to the slurry bed.
  • Both of these patents use magnetic force to accelerate the separation of solid catalyst particles from the slurry.
  • the catalyst is always in a magnetic field, and the magnetic Fischer-Tropsch catalyst is easily magnetized to aggregate and agglomerate, reducing the overall performance of the catalyst.
  • the present invention is directed to the above technical problem, and provides a device and a method for separating a catalyst and a heavy hydrocarbon in a slurry bed reactor, which can achieve high solid-liquid separation efficiency, does not block the filter medium, and separates the solid catalyst.
  • the slurry bed reactor can be operated continuously in industrial applications.
  • a separation device for catalyst and heavy hydrocarbon in a slurry bed reactor designed by the present invention comprises a filter tank, a sieve plate, an electromagnet and a filtrate tank, wherein the filter tank has a slurry inlet a gas outlet, a high pressure gas inlet, a recoil fluid inlet, a catalyst outlet, and a filtrate are circulated back to the input port, the catalyst outlet of the canister is connected to the input end of the filtrate tank, and the output end of the filtrate tank is connected to the filtrate of the filter tank to be recycled.
  • the input port, the output end of the filtrate tank and the pipeline between the filtrate of the filter tank and the inlet of the filter tank are connected with a product delivery pipe connected to the product storage tank, and the catalyst discharge port of the filter tank is also connected with a catalyst discharge pipe. ;
  • a sieve plate is disposed on a lower portion of the filter can, and a magnetic filter medium layer is disposed on the sieve plate, and an electromagnet is disposed on the filter can, and the electromagnet can form a uniform magnetic field on the sieve plate.
  • a method for separating a catalyst from a heavy hydrocarbon by using a catalyst and a heavy hydrocarbon separation device in the above slurry bed reactor comprising the steps of:
  • Step 1 Turn on the electromagnet to form a uniform magnetic field on the sieve plate.
  • the magnetic filter medium is deposited on the sieve plate by the magnetic force. Open the valve HV-1 and introduce the slurry with the solid catalyst in the reactor into the filter tank through the slurry inlet. in;
  • Step 2 When the slurry with the solid catalyst passes through the magnetic filter medium, the solid catalyst particles in the slurry gradually fill the gap between the filter media, and at the same time, since the magnetic filter medium is in an electromagnetic field, the slurry The solid catalyst is magnetically attracted by the surface of the magnetic filter medium, accelerates the aggregation speed of the solid catalyst on the surface of the magnetic filter medium, and gradually forms a filter cake; and the liquid passes through the magnetic filter medium and the filter cake to enter the bottom of the filter tank;
  • Step 3 Open the valve HV-8 and introduce the filtrate at the bottom of the filter tank into the filtrate tank through the catalyst outlet.
  • the valve HV-4 When the liquid level in the filtrate tank no longer increases, open the valve HV-4, and circulate the filtrate through the filtrate through the circulation pump. Returning the input port to the filter tank, repeating the process until the solid content of the filtrate is less than 100 ppm, opening the valve HV-5 to introduce the filtrate into the product storage tank;
  • Step 4 The solid catalyst forms a catalyst filter cake on the magnetic filter medium, and then closes the electromagnet, and opens the valve HV-6 to introduce a liquid fluid through the recoil fluid inlet.
  • the liquid fluid is a Fischer-Tropsch light oil having a boiling point of less than 200 ° C.
  • the catalyst cake and the magnetic filter medium are immersed in the liquid fluid; then the gaseous fluid is introduced through the recoil fluid inlet, and the magnetic filter medium and the catalyst cake are dissipated by the gaseous fluid, in the process of dispersing the magnetic filter medium and the catalyst cake.
  • the magnetic filter medium gradually floats up to the liquid surface, and the solid catalyst particles gradually sink to the bottom of the filter tank;
  • Step 5 Open the valve HV-3 to introduce high pressure gas through the high pressure gas inlet, and open the valve HV-7 to discharge the catalyst and liquid fluid in the filter tank through the catalyst outlet to discharge the filter tank, that is, complete separation of the catalyst from the heavy hydrocarbon.
  • the present invention has the following advantages:
  • the invention adopts dynamic filtration method to separate heavy hydrocarbons from solid catalysts in the Fischer-Tropsch reaction process, and has large treatment capacity, high separation effect, mild filtration conditions, and simple and easy equipment manufacturing.
  • the filter of the present invention uses a dynamic filtration method to separate the solid catalyst in the slurry, and the filter is not clogged by the fine particles and fails, so that the reaction process can be continuously performed.
  • the filtration method of the present invention does not affect the performance of the Fischer-Tropsch catalyst, and the catalyst obtained after filtration is directly returned to the reactor directly in the reactor to participate in the catalytic reaction.
  • the electromagnet on the filter of the present invention acts directly on the filter medium, and the action time is short, and the catalyst is not magnetized to aggregate into large particles to reduce the overall catalytic effect of the catalyst, so that no additional degaussing process is required.
  • the filter and the filtering method of the invention have wide applicability and can be adapted to separate solids and liquids with different particle diameters.
  • Figure 1 is a schematic view of the structure of the present invention
  • FIG. 2 is a schematic structural view of a catalyst cake formed according to the present invention.
  • Figure 3 is a schematic view showing the structure of the catalyst of the present invention separated from the filter medium.
  • 1 - filter tank 1.1 - slurry inlet, 1.2 - gas outlet, 1.3 - high pressure gas inlet, 1.4 - recoil fluid inlet, 1.5 - catalyst outlet, 1.6 - filtrate return to the inlet, 1.7 - catalyst discharge , 1.8—product conveying pipe, 2-screening plate, 3-electromagnet, 4-filtrate tank, 5-product storage tank, 6-magnetic filter medium layer, 7-cycle pump, 8-catalyst filter cake.
  • the catalyst outflow port 1.5 of the canister 1 is connected to the input end of the filtrate tank 4, and the filtrate tank 4
  • the filtrate connected to the filter tank 1 at the output end is circulated back to the input port 1.6, and the output end of the filtrate tank 4 and the filtrate circulating back to the input port 1.6 of the canister 1 are connected to a product conveying pipe connected to the product storage tank 5.
  • the catalyst canister 1 of the filter canister 1 is also connected to a catalyst discharge pipe 1.7;
  • the lower part of the canister 1 is provided with a sieve plate 2, and the sieve plate 2 is provided with a magnetic filter medium layer 6, and the filter can 1 is provided with an electromagnet 3, which can form a uniform on the sieve plate 2.
  • the magnetic field allows the filter medium to be evenly deposited on the sieve plate to ensure that the slurry does not form a channel when it passes through the filter medium, which affects the filtration effect.
  • the sieve plate 2 is located at any position within 1/3 to 2/3 of the height of the canister 1, preferably 1/2 of the height of the canister.
  • the slurry inlet 1.1 is provided with a valve HV-1
  • the gas outlet 1.2 is provided with a valve HV-2
  • the high pressure gas inlet 1.3 is provided with a valve HV-3
  • the recoil fluid inlet 1.4 is provided with a valve.
  • HV-6 a valve HV-8 is arranged on the pipeline between the catalyst outlet port 1.5 and the input end of the filtrate tank 4, the filtrate is circulated back to the input port 1.6 and the valve HV-4 is arranged, and the catalyst discharge pipe 1.7 is provided with a valve HV- 7.
  • the product delivery pipe 1.8 is provided with a valve HV-5.
  • the output end of the filtrate tank 4 is connected to the filtrate of the filter tank 1 through a circulation pump 7. Loop back to the input.
  • the magnetic filter medium layer 6 is iron, cobalt, nickel, or an alloy containing one or more of iron, cobalt, and nickel.
  • the above materials can be attracted by the magnet.
  • the diameter D of the maximum projection surface (the largest cross section of the filter medium) of the magnetic filter medium in the magnetic filter medium layer 6 is preferably 310 ⁇ m ⁇ D ⁇ 10000 ⁇ m. Since the diameter of the catalyst particles is less than 300 ⁇ m, the diameter of the filter medium is larger than 310 ⁇ m, the diameter of the filter is too large, the voids are relatively large after the accumulation, and the catalyst particles are easily penetrated, failing to achieve the filtration effect.
  • the outer surface of the magnetic filter medium in the magnetic filter medium layer 6 is a bare outer surface, or a corrosion-resistant protective film is coated, and the corrosion-resistant protective film is made of polytetrafluoroethylene or polypropylene. (PP, Polypropylene) or ceramic or rubber.
  • the above materials are inert materials and do not react with other materials in the reactor.
  • the shape of the magnetic filter medium in the magnetic filter medium layer 6 is a sphere or a tetrahedron or a cubic or irregular polyhedral particle, and the density ⁇ of the magnetic filter medium in the magnetic filter medium layer 6 is not More than 10g/cm 3 .
  • a preferred range is 0.1 g/cm 3 ⁇ ⁇ ⁇ 1.1 g/cm 3 . This density must be less than the density of the slurry in the kettle, otherwise it cannot float.
  • the mesh diameter of the sieve plate 2 is larger than the diameter of the catalyst monomer in the filter can 1 and smaller than the diameter of the filter medium monomer in the magnetic filter medium layer 6, preferably in the range of 300 ⁇ m ⁇ L ⁇ 9000 ⁇ m;
  • the total thickness of the magnetic filter medium layer 6 deposited thereon ranges from 0.01 m to 1 m.
  • the preferred range is from 0.05 m to 0.5 m, and the above range can ensure the slurry flow rate of the filtered filter medium and the pressure drop during the filtration process.
  • the filtration flux is large and the pressure drop is small, but the filtration effect is not good.
  • the above catalyst is a cobalt-based catalyst, an iron-based catalyst or other Fischer-Tropsch synthetic metal catalyst applied to the Fischer-Tropsch synthesis reaction.
  • a method for separating a catalyst from a heavy hydrocarbon by using a catalyst and a heavy hydrocarbon separation device in the above slurry bed reactor comprising the steps of:
  • Step 1 Turn on the electromagnet 3 to form a uniform magnetic field on the sieve plate 2.
  • the magnetic filter medium is deposited on the sieve plate by the magnetic force (as shown in Fig. 1), and the valve HV-1 is opened to have a solid in the reactor.
  • a slurry of the catalyst is introduced into the canister 1 through the slurry inlet 1.1;
  • Step 2 When the slurry with the solid catalyst passes through the magnetic filter medium, the solid catalyst particles in the slurry gradually fill the gap between the filter media, and at the same time, since the magnetic filter medium is in an electromagnetic field, the slurry The solid catalyst is magnetically attracted by the surface of the magnetic filter medium, accelerates the aggregation speed of the solid catalyst on the surface of the magnetic filter medium, and gradually forms a filter cake; and the liquid passes through the magnetic filter medium and the filter cake to enter the bottom of the filter tank 1;
  • Step 3 Open the valve HV-8 and introduce the filtrate at the bottom of the filter tank 1 into the filtrate tank 4 through the catalyst outflow port 1.5.
  • the valve HV-4 is opened, and the circulation pump 7 is passed.
  • the filtrate is recirculated into the filter tank 1 through the filtrate circulation back to the inlet port 1.6, and the process is repeated until the solid content in the filtrate is detected to be less than 100 ppm, the valve HV-5 is opened to introduce the filtrate into the product storage tank 5; during the filtration process, High pressure gas can be introduced through valve HV-3 to increase the pressure difference and speed up the filtration rate;
  • Step 4 The solid catalyst forms a catalyst cake 8 on the magnetic filter medium (as shown in FIG. 2), then closes the electromagnet 3, and opens the valve HV-6 to introduce a liquid fluid through the recoil fluid inlet 1.4.
  • the liquid fluid has a boiling point lower than that.
  • the Fischer-Tropsch light oil at 200 ° C immerses the catalyst cake 8 and the magnetic filter medium in a liquid fluid; then introduces a gaseous fluid through the recoil fluid inlet 1.4 (gas fluid contains: H 2 , N 2 , CO, Fischer-Tropsch reaction feed gas and Fischer-Tropsch reaction tail gas), using a gaseous fluid to disperse the magnetic filter medium and the catalyst filter cake 8, during the process of dispersing the magnetic filter medium and the catalyst cake 8, magnetic filtration
  • the medium gradually floats up to the liquid level, and the solid catalyst particles gradually sink to the bottom of the filter tank (as shown in Figure 3);
  • Step 5 Open the valve HV-3 and introduce a high pressure gas of 0.1 to 10 MPa through the high pressure gas inlet 1.3.
  • the high pressure gas is one of H 2 , N 2 , CO, Fischer-Tropsch reaction feed gas, and Fischer-Tropsch reaction tail gas, and opens the valve.
  • HV-7 discharges the catalyst and liquid fluid in the canister 1 through the catalyst outlet 1.5 to complete the separation of the catalyst from the heavy hydrocarbons. After the step 5, the canister enters the next cycle.
  • the subsequent reactor may be directly introduced into the catalytic reaction, or may be introduced into the subsequent catalyst recovery tank for storage, and the subsequent treatment is performed, and the liquid fluid is gradually vaporized and separated from the slurry in the reaction vessel after entering the subsequent reactor. After that, recycle it.
  • Formulation slurry I 200 kg of solid catalyst particles having a diameter distribution ranging from 1 to 100 ⁇ m were added to 1 m 3 of the Fischer-Tropsch heavy hydrocarbon to obtain a slurry I.
  • Formulation slurry II 200 kg of solid catalyst particles having a diameter distribution range of 1 to 200 ⁇ m were added to 1 m 3 of the Fischer-Tropsch heavy hydrocarbon to obtain a slurry II.
  • Formulation slurry III 200 kg of solid catalyst particles having a diameter distribution range of 1 to 300 ⁇ m were added to 1 m 3 of the Fischer-Tropsch heavy hydrocarbon to obtain a slurry III.
  • the filter tank 1 has a cross-sectional diameter of 1 m, a height of 3 m and a volume of 2 m 3 ;
  • the filter medium is a hollow iron sphere having a diameter of 310 ⁇ m and a density of 0.1 g/cm 3 , and the sphere is coated with a layer of polytetrafluoroethylene material;
  • the sieve plate 2 is located at the filter.
  • the mesh size of the sieve plate 2 is 300 ⁇ m; the thickness of the filter medium deposited on the sieve plate 2 is 0.05 m.
  • the electromagnet 3 is turned on, so that the magnetic filter medium is densely and evenly accumulated on the sieve plate 2 in the canister 1, and the valve HV-1 is opened to introduce the slurry I into the canister 1.
  • valve HV-1 closes the valve HV-1, open the valve HV-8, and let the filtrate enter the filtrate tank 4.
  • the valve HV-4 is opened.
  • the circulation pump 7, the filtrate is reintroduced into the filter tank 1, and the circulation filtration is carried out.
  • the valve HV-3 is opened to introduce a high pressure gas of 0.2 MPa to increase the filtration pressure difference and accelerate the filtration rate;
  • the high pressure gas is introduced through the valve HV-3, and the catalyst in the filter tank 1 and the Fischer-Tropsch light oil are discharged from the filter tank 1 through the valve HV-7.
  • the filter tank 1 has a cross-sectional diameter of 1 m, a height of 3 m, and a volume of 2 m 3 ;
  • the filter medium is a hollow cobalt tetrahedron having a projection surface diameter of 1000 ⁇ m and a density of 0.5 g/cm 3 , and the tetrahedron is coated with a layer of polypropylene material;
  • the sieve plate 2 Located in the lower part of the filter tank, the mesh size of the sieve plate 2 is 800 ⁇ m; the thickness of the filter medium accumulated on the sieve plate 2 is 0.25 m;
  • the high pressure gas is introduced through the valve HV-3, and the catalyst in the filter tank 1 and the Fischer-Tropsch light oil are discharged from the filter tank 1 through the valve HV-7.
  • the filter tank 1 has a cross-sectional diameter of 1 m, a height of 3 m and a volume of 2 m 3 ;
  • the filter medium is a hollow nickel cube with a projection surface diameter of 6000 ⁇ m and a density of 1.1 g/cm 3 , and the cube is covered with a layer of ceramic material;
  • the sieve plate 2 is located in the filter tank 1 lower portion, the mesh size of the sieve plate 2 is 4000 ⁇ m; the thickness of the filter medium deposited on the sieve plate 2 is 0.5 m.
  • the high pressure gas is introduced through the valve HV-3, and the catalyst in the filter tank 1 and the Fischer-Tropsch light oil are discharged from the filter tank 1 through the valve HV-7.
  • the filter can 1 has a cross-sectional diameter of 1 m, a height of 3 m, and a volume of 2 m 3 ;
  • the filter medium is a hollow nickel cube having a projection surface diameter of 10000 ⁇ m and a density of 0.8 g/cm 3 , and the cube is covered with a rubber material;
  • the sieve plate 2 is located in the filter can. In the lower part, the sieve plate 2 has a mesh diameter of 9000 ⁇ m; the thickness of the filter medium deposited on the sieve plate is 0.5 m.
  • the electromagnet 3 is turned on, so that the magnetic filter medium is uniformly deposited on the sieve plate 2 in the canister 1, and the slurry I is introduced into the canister 1 through the valve HV-1;
  • the high pressure gas is introduced through the valve HV-3, and the catalyst in the filter tank 1 and the Fischer-Tropsch light oil are discharged from the filter tank 1 through the valve HV-7.
  • the filter tank 1 has a cross-sectional diameter of 1 m, a height of 3 m and a volume of 2 m 3 ;
  • the filter medium is a hollow irregular polyhedral iron alloy particle having a projection surface diameter of 2000 ⁇ m and a density of 1.0 g/cm 3 , and the iron alloy particles are resistant to acid and alkali corrosion;
  • the mesh size of the sieve plate 2 is 1500 ⁇ m; the thickness of the filter medium deposited on the sieve plate 2 is 0.15 m.
  • the electromagnet 3 is turned on, so that the magnetic filter medium is densely and uniformly accumulated on the sieve plate 2 in the canister 1, and the slurry II is introduced into the canister 1 through the valve HV-1;
  • the high pressure gas is introduced through the valve HV-3, and the catalyst in the filter tank 1 and the Fischer-Tropsch light oil are discharged from the filter tank 1 through the valve HV-7.
  • the filter tank 1 has a cross-sectional diameter of 1 m, a height of 3 m and a volume of 2 m 3 ;
  • the filter medium is a hollow irregular polyhedral iron alloy particle having a projection surface diameter of 500 ⁇ m and a density of 0.9 g/cm 3 , and the iron alloy particles are resistant to acid and alkali corrosion;
  • the sieve plate 2 is located in the filter can. 1 lower part, the mesh size of the sieve plate 2 is 400 ⁇ m; the thickness of the filter medium deposited on the sieve plate 2 is 0.2 m.
  • the electromagnet 3 is turned on, so that the magnetic filter medium is densely and uniformly accumulated on the sieve plate 2 in the canister 1, and the slurry III is introduced into the canister 1 through the valve HV-1;
  • the high pressure gas is introduced through the valve HV-3, and the catalyst in the filter tank 1 and the Fischer-Tropsch light oil are discharged from the filter tank 1 through the valve HV-7.
  • the filter tank has a cross-section diameter of 1 m, a height of 3 m and a volume of 2 m 3 ;
  • the filter medium is a hollow iron sphere with a projection surface diameter of 800 ⁇ m and a density of 0.7 g/cm 3 , and the iron sphere is covered with a layer of polytetrafluoroethylene;
  • the sieve plate 2 is located at the filter.
  • the mesh size of the sieve plate 2 is 500 ⁇ m; the thickness of the filter medium deposited on the sieve plate 2 is 0.3 m.
  • the electromagnet 3 is turned on, so that the magnetic filter medium is densely and uniformly accumulated on the sieve plate 2 in the canister 1, and the slurry III is introduced into the canister 1 through the valve HV-1;
  • the high pressure gas is introduced through the valve HV-3, and the catalyst in the filter tank 1 and the Fischer-Tropsch light oil are discharged from the filter tank 1 through the valve HV-7.
  • a metal sintered filter plate was installed at the position of the sieve plate 2, and the filter plate was 25 ⁇ m.
  • Example 2 Example 3, Example 4, and Example 5 use a filter medium of a larger size, and the separation effect on the same slurry is inferior to that of Example 1, Example 6, and Example 7, but if the number of cycles of filtration is increased
  • the same effects as in the first embodiment, the sixth embodiment, and the seventh embodiment can be achieved. This is because the size of the pores formed between the large-sized filter media is large, the blocking effect on the solid catalyst in the slurry III is weakened, and the speed at which the solid catalyst forms a filter cake on the filter medium is reduced, so the embodiment 2, the embodiment 3.
  • Example 4 and Example 5 are more suitable for the separation of solids and slurries of larger particles.
  • the filtration method of the present invention is more efficient than the conventional metal sintered filter, and the filtration pressure difference and the reverse stamping difference are smaller than those of the conventional metal sintered filter, so the filtration condition is milder.
  • the main advantage is that the filter of the present invention is not blocked, and the conventional metal sintered filter has a short service life and cannot guarantee the continuous operation of the reactor.

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  • Water Supply & Treatment (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un dispositif de séparation pour un catalyseur et un hydrocarbure lourd dans un réacteur à combustible en suspension. Le dispositif de séparation comprend un réservoir de filtre (1), un plateau perforé (2), un électroaimant (3) et un réservoir de filtrat (4). Une sortie de catalyseur du réservoir de filtre (1) est raccordée à une extrémité d'entrée du réservoir de filtrat (4). Une extrémité de sortie du réservoir de filtrat (4) est raccordée à une entrée de retour de circulation de filtrat du réservoir de filtre (1). Un pipeline entre l'extrémité de sortie du réservoir de filtrat (4) et l'entrée de retour de circulation de filtrat du réservoir de filtre (1) est en communication avec un tuyau de transport de produit d'un réservoir de stockage de produit (5). La sortie de catalyseur du réservoir de filtre (1) est en outre raccordée à un tuyau de décharge de catalyseur. Une partie inférieure à l'intérieur du réservoir de filtre (1) est dotée du plateau perforé (2), sur lequel une couche de support de filtre magnétique (6) est disposée. Le réservoir de filtre (1) est doté de l'électroaimant (3), qui génère un champ magnétique uniforme au niveau du plateau perforé (2). Le dispositif de séparation permet une séparation solide-liquide hautement efficace sans bloquer un milieu filtrant, et un catalyseur solide séparé peut être recyclé et réutilisé, ce qui permet à un réacteur à combustible en suspension de fonctionner en continu dans des applications industrielles.
PCT/CN2017/078014 2016-04-20 2017-03-24 Dispositif et procédé de séparation pour catalyseur et hydrocarbure lourd dans un réacteur à combustible en suspension WO2017181814A1 (fr)

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