CN106669552B - Slurry bed reaction device for preparing liquid fuel from biomass synthesis gas and use method thereof - Google Patents
Slurry bed reaction device for preparing liquid fuel from biomass synthesis gas and use method thereof Download PDFInfo
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- 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
- B01J8/224—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 the particles being subject to a circulatory movement
- B01J8/226—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 the particles being subject to a circulatory movement internally, i.e. the particles rotate within the vessel
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
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- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1854—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement inside the reactor to form a loop
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- B01J8/1872—Details of the fluidised bed reactor
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- 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
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- C10G2/342—Apparatus, reactors with moving solid catalysts
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- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00141—Coils
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
- B01J2208/00831—Stationary elements
- B01J2208/0084—Stationary elements inside the bed, e.g. baffles
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
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Abstract
The invention discloses a slurry bed reaction device for preparing liquid fuel from biomass synthesis gas and a method thereof, wherein the device comprises a slurry bed reactor shell, a cooling coil, a gas distributor, a solid-liquid separator positioned above the inside of the slurry bed reactor shell and the like, the device utilizes a middle-layer gas distributor and a bottom-layer gas distributor to perform circulating flow on the biomass synthesis gas so as to promote uniform distribution of catalyst particles in slurry, utilizes the cooling coil to remove heat released by Fischer-Tropsch synthesis reaction, utilizes the solid-liquid separator to separate liquid products from catalytic particles in the slurry, and utilizes high-pressure N 2 to perform back flushing on the solid-liquid separator so as to remove residual catalyst particles in the solid-liquid separator.
Description
Technical Field
The invention relates to the field of Fischer-Tropsch synthesis, in particular to a slurry bed reaction device suitable for preparing liquid fuel from biomass synthesis gas and a using method thereof.
background
energy is the basis that modern society relies on survival and development, and the supply capacity of clean fuel is the sustainable development of national economy, is one of the basis of national strategic safety guarantee. The biomass is the only carbon resource in renewable energy sources which can be converted into liquid fuel, and can make up for the shortage of petroleum resources on a scale. The liquid fuel is prepared by utilizing the biomass, so that the dependence on fossil energy can be reduced, and the energy can reduce the atmospheric pollution and the emission of greenhouse gases.
A technology for synthesizing liquid fuel by gasifying biomass is characterized by that it uses thermochemical method to gasify biomass to produce raw gas, then uses gas purification and component modulation to obtain high-quality synthetic gas, then uses catalytic technology to synthesize liquid fuel and chemicals after pressurization. The Fischer-Tropsch synthesis reactor is a core reactor of a biomass synthesis liquid fuel technology, and the Fischer-Tropsch synthesis reactor has been reported to have various forms, including a fixed bed, a fluidized bed, a slurry bed and the like. The Fischer-Tropsch synthesis reaction is a reaction with large heat release, and the fixed bed reactor has the defects of difficult heat dissipation, easy catalyst coking and relatively difficult amplification. The fluidized bed reactor has the problems of difficult control of the fluidization process, low catalyst utilization rate, easy abrasion and the like. Compared with the prior art, the slurry bed reactor has the advantages of uniform and controllable temperature, easy control of gas velocity operation and on-line loading and unloading of the catalyst, and is widely applied to the Fischer-Tropsch synthesis reaction of the coal/biomass-based synthesis gas. Slurry bed reactions involve heat and mass transfer between the gas-liquid-solid three phases, so that uniform mixing and suspension of catalyst particles in the slurry is the basis for efficient reactions. The existing slurry bed reactor has the problems that catalyst particles are easy to deposit and agglomerate at the bottom of a slurry bed layer of the slurry bed reactor, so that the density distribution of the catalyst in slurry is uneven, and the heat transfer, mass transfer and reaction of the slurry bed reactor are influenced. In addition, the liquid product, which has a high molecular weight and a high boiling point during the fischer-tropsch synthesis reaction, is generally accumulated in a liquid state inside the reactor, and it is periodically discharged from the reactor to ensure the normal operation of the slurry bed reactor. To avoid catalyst loss, the catalyst particles need to be separated from the liquid product wax and returned to the reactor. Therefore, the design of the solid-liquid separator becomes very important. The common solid-liquid separator at present has the problems that catalyst particles are damaged easily to block a filter member of the separator, so that the reactor stops, and the like.
Therefore, in order to improve the reaction efficiency of the fischer-tropsch synthesis and reduce the loss of the catalyst, it is necessary to develop a slurry bed reactor having good catalyst-slurry mixing, suspension effects and solid-liquid separation efficiency.
Disclosure of Invention
the invention aims to overcome the defects and provide a slurry bed reaction device and a method which can effectively enhance the circulating flow of biomass synthesis gas in a slurry bed reactor, promote the uniform mixing and suspension of catalyst particles in slurry and facilitate the separation of Fischer-Tropsch synthesis liquid products and the catalyst particles.
The invention is realized by the following technical scheme:
2a slurry bed reaction device for preparing liquid fuel from biomass synthesis gas comprises a slurry bed reactor shell, wherein a solid-liquid separator, a middle-layer gas distributor and a bottom-layer gas distributor are sequentially arranged in the slurry bed reactor shell from top to bottom, a catalyst feed port is arranged on the slurry bed reactor shell and close to the bottom end of the solid-liquid separator, a synthesis gas upper end air inlet is arranged at the joint of the slurry bed reactor shell and the middle-layer gas distributor, a top exhaust port is arranged at the top end of the slurry bed reactor shell, a slurry discharge port is arranged at the bottom end of the slurry bed reactor shell, a synthesis gas lower end air inlet is arranged at the lower end of the slurry bed reactor shell, cooling coils are arranged in the slurry bed reactor shell, below the catalyst feed port and above the bottom-layer gas distributor, a cooling water inlet and a cooling water outlet of each cooling coil are located outside the slurry bed reactor shell, the cooling water outlet is located above the cooling water inlet, a liquid outlet communicated with the outside is arranged on the solid-liquid separator.
The slurry bed reactor shell comprises a cylindrical main body, and spherical covers are respectively arranged at the upper end and the lower end of the cylindrical main body.
the bottom end of the solid-liquid separator is positioned at 2/3-3/4 of the height of the slurry bed reactor; the solid-liquid separator is a sealed cylindrical structure formed by spherical grids, and the aperture of each spherical grid is 0.1-0.2 um;
(II) the middle-layer gas distributor consists of a plurality of concentric annular pipelines; air distribution holes with upward openings are uniformly distributed on each concentric ring; the middle-layer gas distributor is provided with a cross-shaped main gas inlet pipe communicated with the concentric annular pipeline; the middle-layer gas distributor is positioned at 1/4-1/3 of the height of the slurry bed reactor;
(III) the bottom layer gas distributor is circular and comprises an upper layer of screen mesh, a lower layer of screen mesh and a purification layer positioned between the upper layer of screen mesh and the lower layer of circular screen mesh; the aperture of the screen mesh is 0.2-0.5 um; the purifying layer is filled with ceramic rings, and the inner diameter of each ceramic ring is 1-3 mm.
The bottom end of the solid-liquid separator is positioned at 2/3 of the height of the slurry bed reactor; the aperture of the spherical grid is 0.1 um;
(II) the middle layer gas distributor is positioned at 1/3 of the height of the slurry bed reactor.
And (III) the aperture size of the screen mesh is 0.2um, and the inner diameter of the ceramic ring is 2 mm.
The cooling coil cooling water inlet is close to the shell of the bottom layer distributor, and the cooling water outlet is at 1/2 of the height of the slurry bed reactor.
A method for preparing liquid fuel slurry bed reactor by using biomass synthesis gas to carry out Fischer-Tropsch synthesis utilizes a middle-layer gas distributor and a bottom-layer gas distributor to carry out circular flow on the biomass synthesis gas so as to promote uniform distribution of catalyst particles in slurry, utilizes a cooling coil to remove heat released by Fischer-Tropsch synthesis reaction, utilizes a solid-liquid separator to separate liquid products and the catalyst particles in the slurry, utilizes high-pressure N 2 to carry out back flushing on the solid-liquid separator, and removes the residual catalyst particles in the solid-liquid separator.
The method comprises the following steps:
opening the upper cover of the shell of the slurry bed reactor, injecting slurry to make the height of the slurry be 1/2-2/3 of the height of the reactor, and covering the upper cover;
Secondly, dividing the biomass synthesis gas into two streams of gas, respectively passing through an upper end gas inlet of the synthesis gas, introducing the lower end gas inlet of the synthesis gas into the slurry bed reactor, wherein the flow ratio of the upper end gas inlet of the synthesis gas to the lower end gas inlet of the synthesis gas is 1/5-1/3, and adjusting the flow ratio of the upper end gas inlet to the lower end gas inlet to control the flowing speed of the synthesis gas in the slurry to enable catalyst particles to be uniformly mixed in the slurry and to be in a suspended state;
Thirdly, the synthesis gas is subjected to Fischer-Tropsch synthesis reaction in a slurry bed reactor to generate a gas product and a liquid product;
Discharging the gaseous product through an exhaust port at the top of the slurry bed reactor, and gradually accumulating the liquid product in the slurry bed reactor;
Fifthly, when the height of the slurry reaches 2/3-3/4 of the height of the reactor, opening an outlet valve of a pipeline of the solid-liquid separator, and discharging the liquid product out of the reactor through the solid-liquid separator under the action of the pressure of the reactor; when the slurry level in the reactor dropped below 2/3 f the reactor level, the solid liquid separator conduit outlet valve was closed;
Sixthly, opening a high-pressure N 2 blowback valve to enable the pressure of a pipeline to be slightly higher than the pressure in the reactor, and blowing the catalyst remained in the solid-liquid separator through N2 to enable catalyst particles to enter slurry of the reactor;
In the process, cooling water enters from the inlet of the cooling coil and is removed from the outlet of the cooling coil, and the temperature of the reactor in the reaction process is regulated by the cooling water;
And seventhly, discharging the slurry from the slurry discharge port after the reaction is finished.
the slurry level in step one is at 1/2, the reactor level.
And in the second step, the flow ratio of the upper end gas inlet of the synthetic gas to the lower end gas inlet of the synthetic gas is 1/4.
the invention has the following beneficial effects:
1) The slurry bed reactor is provided with two gas distributors, the bottom layer gas distributor is of a screen-shaped structure, so that the biomass synthesis gas can uniformly pass through the bottom layer gas distributor, and catalyst particles in slurry flow and are suspended in the slurry under the driving action of airflow; catalyst particles on the upper part of the slurry can gradually settle due to the action of gravity, so that the density of the catalyst particles in the slurry is easily uneven; the middle-layer gas distributor is arranged in the slurry bed reactor and is in a concentric ring structure, so that catalyst particles falling in slurry can flow again, the flow state of the synthesis gas in the slurry in the reactor can be adjusted by controlling the flow of the upper end inlet and the lower end inlet of the synthesis gas, the catalyst is in a uniform distribution and suspension state in the slurry, and the heat transfer, mass transfer and reaction efficiency of the slurry bed reactor are promoted.
2) The solid-liquid separator is arranged above the inside of the slurry bed reactor, so that liquid products and catalyst particles in the slurry bed reactor can be directly separated, the grid structure of the solid-liquid separator is smaller than the catalyst particles, most of the catalyst and the liquid products can be separated and return to slurry in the reactor, catalyst powder crushed by collision in the slurry bed reactor enters the reactor through the high-pressure N 2 in a back blowing mode, the blockage of the solid-liquid separator due to the fact that the catalyst powder is retained in the solid-liquid separator is avoided, and the catalyst utilization rate and the solid-liquid separation effect are improved.
drawings
FIG. 1 is a schematic diagram of the structure of a slurry bed reactor of the present invention;
FIG. 2 is a schematic diagram of the solid-liquid separator of FIG. 1;
FIG. 3 is the bottom layer gas distributor of FIG. 1;
FIG. 4 is a middle layer gas distributor of FIG. 1;
The device comprises a slurry bed reactor shell, a solid-liquid separator, a catalyst feeding hole, a synthesis gas upper end air inlet, a synthesis gas lower end air inlet, a synthesis gas bottom end air distributor, a synthesis gas middle layer air distributor, a synthesis gas discharging hole, a synthesis gas outlet, a cooling water inlet, a cooling water outlet, a cooling coil, a top exhaust port, a cooling liquid outlet, a high-pressure N2 back flushing port, a cooling coil, a circular screen mesh, a ceramic ring, a main air inlet pipe, a main.
Detailed Description
the invention is further illustrated by the following examples and figures.
A slurry bed reaction device for preparing liquid fuel from biomass synthesis gas comprises a slurry bed reactor shell 1, wherein a solid-liquid separator 2, a middle-layer gas distributor 7 and a bottom-layer gas distributor 6 are sequentially arranged in the slurry bed reactor shell 1 from top to bottom; a catalyst feed port 3 is arranged on the slurry bed reactor shell 1 and close to the bottom end of the solid-liquid separator 2; a gas inlet 4 at the upper end of the synthesis gas is arranged at the joint of the slurry bed reactor shell 1 and the middle layer gas distributor 7; the top end of the slurry bed reactor shell 1 is provided with a top exhaust port 11, the bottom end is provided with a slurry outlet 8, and the lower end is provided with a synthesis gas lower end air inlet 5; a cooling coil 14 is arranged in the slurry bed reactor shell 1, below the catalyst feed port 3 and above the bottom layer gas distributor 6; the cooling water inlet 9 and the cooling water outlet 10 of the cooling coil 14 are both positioned outside the slurry bed reactor shell 1, and the cooling water outlet 10 is positioned above the cooling water inlet 9; a liquid outlet pipe 12 communicated with the outside is arranged on the solid-liquid separator 2; the outlet end of the liquid outlet pipe 12 positioned outside the slurry bed reactor shell 1 is provided with a high-pressure N2 blowback port 13.
The slurry bed reactor shell 1 comprises a cylindrical main body, and spherical covers are respectively arranged at the upper end and the lower end of the cylindrical main body.
The bottom end of the solid-liquid separator 2 is positioned at 2/3-3/4 of the height of the slurry bed reactor; the solid-liquid separator 2 is a sealed cylindrical structure formed by spherical grids, and the aperture of each spherical grid is 0.1-0.2 um;
The middle layer gas distributor 7 consists of a plurality of concentric annular pipelines; air distribution holes 72 with upward openings are uniformly distributed on each concentric ring; a cross-shaped main air inlet pipe 71 communicated with the concentric annular pipeline is arranged on the middle-layer gas distributor 7; the middle layer gas distributor 7 is positioned at 1/4-1/3 of the height of the slurry bed reactor;
The bottom layer gas distributor 6 is circular and comprises an upper layer of screen 61, a lower layer of screen 61 and a purification layer positioned between the upper layer of circular screen 61 and the lower layer of circular screen; the aperture of the screen 61 is 0.2-0.5 um; the purifying layer is filled with ceramic rings, and the inner diameter of each ceramic ring is 1-3 mm.
The bottom end of the solid-liquid separator is positioned at 2/3 of the height of the slurry bed reactor; the aperture of the spherical grid is 0.1 um;
the middle gas distributor 7 is located at 1/3 of the height of the slurry bed reactor.
the aperture size of the screen 61 is 0.2um, and the inner diameter of the ceramic ring is 2 mm.
The cooling coil 14 has a cooling water inlet 9 near the shell of the bottom distributor and a cooling water outlet 10 at 1/2 at the height of the slurry bed reactor.
a method for preparing liquid fuel slurry bed reactor by using biomass synthesis gas to carry out Fischer-Tropsch synthesis utilizes a middle-layer gas distributor and a bottom-layer gas distributor to carry out circular flow on the biomass synthesis gas so as to promote uniform distribution of catalyst particles in slurry, utilizes a cooling coil to remove heat released by Fischer-Tropsch synthesis reaction, utilizes a solid-liquid separator to separate liquid products and the catalyst particles in the slurry, utilizes high-pressure N 2 to carry out back flushing on the solid-liquid separator, and removes the residual catalyst particles in the solid-liquid separator.
The method comprises the following steps:
opening the upper cover of the shell of the slurry bed reactor, injecting slurry to make the height of the slurry be 1/2-2/3 of the height of the reactor, and covering the upper cover;
secondly, dividing the biomass synthesis gas into two gas streams, respectively passing through a synthesis gas upper end gas inlet 4 and a synthesis gas lower end gas inlet 5, introducing the two gas streams into the slurry bed reactor, wherein the flow ratio of the synthesis gas upper end gas inlet 4 to the synthesis gas lower end gas inlet 5 is 1/5-1/3, and adjusting the flow ratio of the upper end gas inlet to the lower end gas inlet to control the flow speed of the synthesis gas in the slurry to enable catalyst particles to be uniformly mixed in the slurry and to be in a suspended state;
thirdly, the synthesis gas is subjected to Fischer-Tropsch synthesis reaction in a slurry bed reactor to generate a gas product and a liquid product;
fourthly, discharging the gaseous product through a gas outlet 11 at the top of the slurry bed reactor, and gradually accumulating the liquid product in the slurry bed reactor;
fifthly, when the height of the slurry reaches 2/3-3/4 of the height of the reactor, opening an outlet valve of a pipeline of the solid-liquid separator, and discharging the liquid product out of the reactor through the solid-liquid separator under the action of the pressure of the reactor; when the slurry level in the reactor dropped below 2/3 f the reactor level, the solid liquid separator conduit outlet valve was closed;
Sixthly, opening a high-pressure N 2 blowback valve to enable the pressure of a pipeline to be slightly higher than the pressure in the reactor, and blowing the catalyst remained in the solid-liquid separator through N 2 to enable catalyst particles to enter slurry of the reactor;
In the process, cooling water enters from the inlet of the cooling coil and is removed from the outlet of the cooling coil, and the temperature of the reactor in the reaction process is regulated by the cooling water;
And seventhly, discharging the slurry from the slurry discharge port after the reaction is finished.
The slurry level in step one is at 1/2, the reactor level.
And in the second step, the flow ratio of the upper end gas inlet 4 of the synthetic gas to the lower end gas inlet 5 of the synthetic gas is 1/4.
As shown in fig. 1, a slurry bed reactor for preparing liquid fuel from biomass synthesis gas comprises a slurry bed reactor shell 1, a solid-liquid separator 2, a cooling coil 14, a bottom layer gas distributor 6, a middle layer gas distributor 7 and the like; the slurry bed reactor shell 1 is cylindrical in main structure, spherical covers are arranged at the upper end and the lower end of the shell, a solid-liquid separator 2 is arranged above the inner portion of the shell, a middle-layer gas distributor 7 and a bottom-layer gas distributor 6 are arranged below the inner portion of the shell, and a cooling coil pipe 14 is arranged between slurry inside the shell and the gas distributors.
the slurry bed reactor shell 1 is vertically arranged, and the lower end of the slurry bed reactor shell is fixed by a base. The side wall of the upper end of the shell 1 of the slurry bed reactor is provided with a catalyst feed port 3, the feed port is positioned on the shell wall near the lower end of the solid-liquid separator and is positioned at 2/3-3/4 of the height of the slurry bed reactor. The catalyst particles and the liquid paraffin are uniformly mixed and then enter the slurry bed reactor through the catalyst feed port 3. The connection part of the reactor shell and the middle layer gas distributor 7 is provided with a synthesis gas upper end gas inlet 4, the side wall of the spherical cover at the lower part of the bottom layer gas distributor 6 is provided with a synthesis gas lower end gas inlet 5, the flow of the biomass synthesis gas at the upper end gas inlet and the lower end gas inlet is controlled by a flow controller, so that the flow ratio of the upper end gas inlet to the lower end gas inlet is 1/5-1/3, and the flow ratio of the upper end gas inlet to the lower end gas inlet is 1/4 in the preferred embodiment. And a top exhaust port 11 and a slurry outlet 8 are respectively arranged at the top end and the bottom end of the shell of the slurry bed reactor, a gas product generated by the Fischer-Tropsch synthesis reaction is discharged through the top exhaust port 11, and the slurry in the slurry bed reactor is discharged through the slurry outlet 8.
The solid-liquid separator 2 is positioned above the inside of the slurry bed reactor shell 1, and the bottom end of the solid-liquid separator is positioned at 2/3-3/4 of the height of the slurry bed reactor. The solid-liquid separator is of a cylindrical structure and consists of spherical grids 21, and the aperture of each grid is 0.1-0.2 um. In a preferred embodiment, the solid liquid separator grid has a pore size of 0.15 um and its bottom end is located at 2/3 at the height of the slurry bed reactor.
the top end of the solid-liquid separator is connected with a pipeline which leads to the outside of the slurry bed reactor and is used for discharging liquid products generated by the Fischer-Tropsch synthesis reaction in the reactor, a liquid outlet 12 is arranged at the outlet of the pipeline, a high-pressure N 2 blowback port 13 is arranged at the outer end of the pipeline, and catalyst particles remained in the solid-liquid separator are blowback into the slurry bed reactor through a high-pressure N 2 blowback port.
The middle layer gas distributor 7 is positioned at the middle lower part in the shell of the slurry bed reactor and is positioned at 1/4-1/3 of the height of the reactor. The middle layer gas distributor consists of distributor subunits with concentric ring structures, and the arc-shaped distribution pipe 72 of each distributor subunit is uniformly distributed with gas distribution holes 73 with upward openings. The biomass synthesis gas enters the slurry bed reactor through the air distribution holes and flows upwards. The middle layer gas distributor is provided with main gas inlet pipes 71 in four directions and used for conveying biomass synthesis gas. In a preferred embodiment, the middle layer gas distributor is located at 1/3 the height of the slurry bed reactor.
The bottom layer gas distributor 6 is located at the joint of the main structure of the slurry bed reactor and the lower end circular cover, is of a circular structure and is divided into three layers, wherein the upper layer and the lower layer are circular screens 61, the aperture of each screen is 0.2-0.5um, the middle layer is filled with ceramic rings 62, and the inner diameter of each ceramic ring is 1-3 mm. In a preferred embodiment, the mesh size of the bottom layer gas distributor screen is 0.2um and the inner diameter of the ceramic ring is 2 mm.
The biomass synthesis gas is divided into two gas streams through the flow controller, and the two gas streams respectively enter from the bottom layer gas distributor and the middle layer gas distributor, the bottom layer gas distributor adopts a screen structure, and the synthesis gas can be uniformly dispersed into the reactor from the bottom to drive the catalyst to flow and disperse in the slurry. Catalyst particles above the slurry can be deposited downwards under the action of gravity, and the synthesis gas in the middle-layer gas distributor flows out from the upper part of the gas distribution port to drive the catalyst to flow upwards. The flow of the biomass synthesis gas in the bottom layer gas distributor and the middle layer gas distributor is adjusted by adjusting the flow controllers, so that the uniform distribution and suspension of the catalyst in the slurry bed reactor are promoted.
the cooling coil 14 is positioned between the slurry in the slurry bed reactor and the gas distributor, the cooling coil is provided with a cooling water inlet 9 at the position close to the shell of the bottom layer gas distributor, and a cooling water outlet 10 is arranged at the position 1/2 at the height of the slurry bed reactor. The temperature of the reactor is controlled by removing the excessive heat released by the Fischer-Tropsch synthesis reaction through a cooling coil.
catalyst particles and liquid paraffin are uniformly mixed to form slurry, the slurry enters the reactor through a feed inlet at the upper end of the slurry bed reactor, the height of the slurry fed into the reactor is 1/2-2/3 of the height of the slurry bed reactor, and in a preferred embodiment, the height of the slurry is 1/2 of the height of the slurry bed reactor.
the implementation method for performing Fischer-Tropsch synthesis on the slurry bed reaction device for preparing the liquid fuel from the biomass synthesis gas comprises the steps of utilizing the slurry bed reactor to perform Fischer-Tropsch synthesis reaction, utilizing a middle-layer gas distributor and a bottom-layer gas distributor to perform circulating flow on the biomass synthesis gas to promote uniform distribution of catalyst particles in slurry, utilizing the cooling coil to remove heat released by the Fischer-Tropsch synthesis reaction, utilizing the solid-liquid separator to separate liquid products from the catalyst particles in the slurry, and utilizing high-pressure N 2 to perform back flushing on the solid-liquid separator to remove residual catalyst particles in the solid-liquid separator.
The operation method for preparing the liquid fuel slurry bed reactor by using the biomass synthesis gas further comprises the following steps: 1) the biomass synthesis gas is divided into two gas streams, the flow of each gas stream is controlled by a flow controller, and the flow ratio of an upper end gas inlet to a lower end gas inlet is 1/5-1/3; 2) the synthesis gas enters slurry inside a slurry bed reactor to drive the slurry to flow, and the flow rate of the synthesis gas in the reactor is controlled by adjusting the flow ratio of an upper end gas inlet and a lower end gas inlet, so that catalyst particles are uniformly mixed in the slurry and are in a suspension state; 3) the synthetic gas reacts with a catalyst in a slurry bed reactor to generate gas and liquid products; 4) the gaseous product is discharged through an exhaust port at the top of the slurry bed reactor, and the liquid product is gradually accumulated in the slurry bed reactor; 5) when the height of the slurry reaches 2/3-3/4 of the height of the reactor, opening an outlet valve of a pipeline of the solid-liquid separator, discharging a liquid product out of the reactor through the solid-liquid separator under the action of the pressure of the reactor, and returning solid particles of the catalyst into the slurry; 6) when the slurry level in the reactor dropped below 2/3 f the reactor level, the solid liquid separator conduit outlet valve was closed; 7) opening a high-pressure N2 back-flushing valve to enable the pressure of a pipeline to be slightly higher than the pressure in the reactor, and blowing the catalyst remained in the solid-liquid separator through N2 to enable catalyst powder to enter slurry of the reactor in a back-flushing mode; in the process, cooling water enters from the inlet of the cooling coil and is removed from the outlet of the cooling coil, and the temperature of the reactor in the reaction process is regulated by the cooling water;
8) after the reaction, the slurry was discharged from the slurry outlet.
It should be understood that parts of the specification not set forth in detail are well within the prior art.
It should be understood that the above description of the preferred embodiments is given for clarity and not for any purpose of limitation, and that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (8)
- 21. a reaction device for preparing liquid fuel slurry bed by biomass synthesis gas is characterized by comprising a slurry bed reactor shell (1), a solid-liquid separator (2) is sequentially arranged in the slurry bed reactor shell (1) from top to bottom, a middle-layer gas distributor (7) and a bottom-layer gas distributor (6) are arranged in sequence, a catalyst feeding port (3) is arranged on the slurry bed reactor shell (1) and close to the bottom end of the solid-liquid separator (2), a synthetic gas upper-end air inlet (4) is arranged at the joint of the slurry bed reactor shell (1) and the middle-layer gas distributor (7), a top exhaust port (11) is arranged at the top end of the slurry bed reactor shell (1), a slurry discharging port (8) is arranged at the bottom end, a synthetic gas lower-end air inlet (5) is arranged at the lower end of the slurry bed reactor shell (1), cooling coils (14) are arranged above the bottom-layer gas distributor (6), cooling water inlets (9) and cooling water outlets (10) of the cooling coils (14) are both positioned outside the slurry bed reactor shell (1), cooling water outlets (10) are positioned above the middle-layer gas distributor (3), a high-0.7), a circular cylindrical slurry bed reactor shell (1) with a cylindrical slurry bed reactor shell (1-7) and a reverse blowing structure, slurry bed reactor shell (360-7), the circular mesh is formed by a cylindrical mesh, the circular mesh of which is arranged at the circular mesh, the circular mesh of the circular mesh structure of which is formed by the circular mesh, the circular mesh openings of the circular mesh, the circular mesh of the circular mesh openings of the circular mesh, the circular.
- 2. The reaction device for preparing the liquid fuel slurry bed by using the biomass synthesis gas as claimed in claim 1, wherein: the slurry bed reactor shell (1) comprises a cylindrical main body, and spherical covers are respectively arranged at the upper end and the lower end of the cylindrical main body.
- 3. The reaction device for preparing the liquid fuel slurry bed by using the biomass synthesis gas as claimed in claim 1, wherein: the bottom end of the solid-liquid separator is positioned at 2/3 of the height of the slurry bed reactor; the aperture of the spherical grid is 0.1 um;(II) the middle layer gas distributor (7) is positioned at 1/3 of the height of the slurry bed reactor; and (III) the aperture size of the screen (61) is 0.2um, and the inner diameter of the ceramic ring is 2 mm.
- 4. The reaction device for preparing the liquid fuel slurry bed by using the biomass synthesis gas as claimed in claim 1, wherein: the cooling coil (14) has a cooling water inlet (9) near the shell of the bottom distributor and a cooling water outlet (10) at 1/2 of the height of the slurry bed reactor.
- 5. A method for carrying out Fischer-Tropsch synthesis by using the biomass synthesis gas-to-liquid fuel slurry bed reaction device as claimed in any one of claims 1 to 4, is characterized in that the biomass synthesis gas is circulated by using a middle layer gas distributor and a bottom layer gas distributor to promote uniform distribution of catalyst particles in slurry, heat released by Fischer-Tropsch synthesis reaction is removed by using the cooling coil, liquid products and the catalyst particles in the slurry are separated by using a solid-liquid separator, and the residual catalyst particles in the solid-liquid separator are removed by carrying out back flushing on the solid-liquid separator by using high-pressure N 2.
- 6. The method of claim 5, comprising the steps of:opening the upper cover of the shell of the slurry bed reactor, injecting slurry to make the height of the slurry be 1/2-2/3 of the height of the reactor, and covering the upper cover;Secondly, dividing the biomass synthesis gas into two gas flows, respectively passing through an upper end gas inlet (4) of the synthesis gas, introducing a lower end gas inlet (5) of the synthesis gas into the slurry bed reactor, wherein the flow ratio of the upper end gas inlet (4) of the synthesis gas to the lower end gas inlet (5) of the synthesis gas is 1/5-1/3, and adjusting the flow ratio of the upper end gas inlet to the lower end gas inlet to control the flowing speed of the synthesis gas in the slurry to enable catalyst particles to be uniformly mixed in the slurry and to be in a suspended state;Thirdly, the synthesis gas is subjected to Fischer-Tropsch synthesis reaction in a slurry bed reactor to generate a gas product and a liquid product;Fourthly, the gaseous product is discharged through a gas outlet (11) at the top of the slurry bed reactor, and the liquid product is gradually accumulated in the slurry bed reactor;Fifthly, when the height of the slurry reaches 2/3-3/4 of the height of the reactor, opening an outlet valve of a pipeline of the solid-liquid separator, and discharging the liquid product out of the reactor through the solid-liquid separator under the action of the pressure of the reactor; when the slurry level in the reactor dropped below 2/3 f the reactor level, the solid liquid separator conduit outlet valve was closed;sixthly, opening a high-pressure N 2 blowback valve to enable the pressure of a pipeline to be slightly higher than the pressure in the reactor, and blowing the catalyst remained in the solid-liquid separator through N 2 to enable catalyst particles to enter slurry of the reactor;in the process, cooling water enters from the inlet of the cooling coil and is removed from the outlet of the cooling coil, and the temperature of the reactor in the reaction process is regulated by the cooling water;and seventhly, discharging the slurry from the slurry discharge port after the reaction is finished.
- 7. the method of claim 6, wherein the slurry level in step one is at 1/2 of the reactor level.
- 8. The method as claimed in claim 6, wherein the flow ratio of the upper end inlet (4) of the synthetic gas and the lower end inlet (5) of the synthetic gas in the second step is 1/4.
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| CN101396647A (en) * | 2007-09-29 | 2009-04-01 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
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| CN101396647A (en) * | 2007-09-29 | 2009-04-01 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
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