CN106669552B - Slurry bed reaction device for preparing liquid fuel from biomass synthesis gas and use method thereof - Google Patents

Abstract

The invention discloses a slurry bed reaction device and method for producing liquid fuel from biomass synthesis gas. The device is composed of a slurry bed reactor shell, a cooling coil, a gas distributor, a solid-liquid separator located above the inside of the slurry bed reactor shell, etc.; the present invention utilizes the middle gas distributor and the bottom gas distributor The biomass synthesis gas is circulated to promote the uniform distribution of catalyst particles in the slurry, the heat released by the Fischer-Tropsch synthesis reaction is removed by using the cooling coil, and the liquid product in the slurry is separated from the catalytic particles by a solid-liquid separator , using high-pressure _N2 to backflush the solid-liquid separator to remove the catalyst particles remaining in the solid-liquid separator. The invention improves the heat transfer, mass transfer and energy conversion efficiency of the slurry bed reactor, and prolongs the service life of the catalyst.

Description

A slurry bed reaction device for preparing liquid fuel from biomass synthesis gas and its application method

technical field

The invention relates to the field of Fischer-Tropsch synthesis, in particular to a slurry bed reaction device suitable for producing liquid fuel from biomass synthesis gas and a use method thereof.

Background technique

Energy is the basis for the survival and development of modern society. The supply capacity of clean fuel is related to the sustainable development of the national economy and is one of the foundations of national strategic security. Biomass is the only carbon resource that can be converted into liquid fuels in renewable energy, which can make up for the shortage of petroleum resources on a large scale. The use of biomass to produce liquid fuels can not only reduce the dependence on fossil energy, but also reduce air pollution and greenhouse gas emissions.

Biomass gasification synthesis of liquid fuel technology refers to the generation of crude gas by gasification of biomass through thermochemical methods, and then high-quality synthesis gas is obtained through gas purification and component modulation, and then pressurized and then catalytic technology is used to synthesize liquid fuels A complete set of integrated technologies for chemicals and chemicals, the products mainly include hydrocarbon fuels (such as gasoline, diesel, etc.) and oxygenated compound liquid fuels (such as low-carbon mixed alcohols and dimethyl ether, etc.), Fischer-Tropsch synthesis technology is the key. Fischer-Tropsch synthesis reactor is the core reactor of biomass synthesis liquid fuel technology. There are various types of Fischer-Tropsch synthesis reactors that have been reported, including fixed bed, fluidized bed and slurry bed. Since the Fischer-Tropsch synthesis reaction is a reaction with a large heat release, and the fixed-bed reactor has difficulty in heat dissipation, it is easy to cause coking of the catalyst, which makes it relatively difficult to scale up the fixed-bed reactor. The fluidized bed reactor has problems such as difficulty in controlling the fluidization process, low utilization rate of the catalyst, and easy wear and tear. In contrast, the slurry bed reactor has the advantages of uniform and controllable temperature, easy control of gas velocity operation, and online loading and unloading of catalysts, so it is widely used in the Fischer-Tropsch synthesis reaction of coal/biomass-based syngas. The slurry bed reaction involves heat and mass transfer between the gas-liquid-solid three-phase, so the uniform mixing and suspension of catalyst particles in the slurry is the basis of efficient reaction. At present, the catalyst particles in the slurry bed reactor are easy to deposit and agglomerate at the bottom of the slurry bed of the slurry bed reactor, resulting in uneven density distribution of the catalyst in the slurry, which affects the heat transfer and mass transfer of the slurry bed reactor. and react. In addition, during the Fischer-Tropsch synthesis reaction, the liquid product usually accumulates in the reactor in a liquid state due to its large molecular weight and high boiling point, and it needs to be discharged from the reactor regularly to ensure the normal operation of the slurry bed reactor. run. 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. However, the current common solid-liquid separators are prone to problems such as catalyst particles being damaged and clogging the filter components of the separator, resulting in shutdown of the reactor.

Therefore, in order to improve the efficiency of Fischer-Tropsch synthesis reaction and reduce the loss of catalyst, it is necessary to develop a slurry bed reactor with good catalyst-slurry mixing, suspension effect and solid-liquid separation efficiency.

Contents of the invention

The object of the present invention is to overcome the above-mentioned defects, provide a kind of can effectively strengthen the circulating flow of biomass synthesis gas in the slurry bed reactor, promote the homogeneous mixing and suspension of catalyst particles in the slurry, and Fischer-Tropsch synthesis liquid product and A slurry bed reaction device and method for easy separation of catalyst particles.

The present invention is achieved through the following technical solutions:

A slurry bed reaction device for preparing liquid fuel from biomass synthesis gas, comprising a slurry bed reactor shell, in which a solid-liquid separator and a middle layer gas distributor are arranged sequentially from top to bottom and the bottom gas distributor; the slurry bed reactor shell is provided with a catalyst feed port near the bottom of the solid-liquid separator; the connection between the slurry bed reactor shell and the middle layer gas distributor is provided with The upper end air inlet of synthesis gas; the top of the slurry bed reactor shell is provided with a top exhaust port, the bottom end is provided with a slurry outlet, and the lower end is provided with a synthesis gas lower end air inlet; the slurry bed reactor A cooling coil is arranged in the shell, below the catalyst feed inlet, and above the bottom gas distributor; the cooling water inlet and cooling water outlet of the cooling coil are located outside the shell of the slurry bed reactor, and the cooling water outlet is located at the cooling Above the water inlet; the solid-liquid separator is provided with a liquid outlet pipe communicating with the outside world; the outlet end of the liquid outlet pipe located outside the slurry bed reactor shell is provided with a high-pressure _N2 blowback port.

The shell of the slurry bed reactor includes a cylindrical main body, and spherical covers are respectively arranged at the upper and lower ends of the cylindrical main body.

(1) The bottom end of the solid-liquid separator is located at 2/3-3/4 of the height of the slurry bed reactor; the solid-liquid separator is a sealed cylindrical structure composed of a spherical grid, and the spherical The mesh aperture is 0.1-0.2 um;

(2) The middle-level gas distributor is composed of several concentric ring-shaped pipes; each of the concentric rings is evenly distributed with air distribution holes opening upward; the middle-level gas distributor is provided with concentric ring-shaped pipes. The cross-shaped main inlet pipe; the middle gas distributor is located at 1/4-1/3 of the height of the slurry bed reactor;

(3) The bottom gas distributor is circular, including upper and lower layers of screens and a purification layer between the upper and lower layers of circular screens; the aperture of the screen is 0.2-0.5 um; the inside of the purification layer is filled with There are ceramic rings, and the inner diameter of the ceramic ring is 1-3 mm.

(1) The bottom end of the solid-liquid separator is located at 2/3 of the height of the slurry bed reactor; the pore size of the spherical mesh is 0.1 um;

(2) The middle layer gas distributor is located at 1/3 of the height of the slurry bed reactor.

(3) The pore size of the screen is 0.2 um, and the inner diameter of the ceramic ring is 2 mm.

The cooling water inlet of the cooling coil is close to the shell of the bottom distributor, and the cooling water outlet is at 1/2 of the height of the slurry bed reactor.

A method for producing liquid fuel by using the above-mentioned biomass synthesis gas in a slurry bed reactor for Fischer-Tropsch synthesis, using a middle layer gas distributor and a bottom gas distributor to circulate the biomass synthesis gas to promote catalyst particles in the slurry Uniform distribution, using the cooling coil to remove the heat released by the Fischer-Tropsch synthesis reaction, using a solid-liquid separator to separate the liquid product from the catalytic particles in the slurry, and using high-pressure N to backflush the solid _- liquid separator to remove Catalyst particles remaining in the solid-liquid separator.

Including the following steps:

1. Open the upper cover of the slurry bed reactor shell, inject the slurry so that its height is at 1/2-2/3 of the reactor height, and close the upper cover;

2. Divide the biomass synthesis gas into two streams, which pass through the upper inlet of the synthesis gas and the lower inlet of the synthesis gas respectively into the slurry bed reactor, the upper inlet of the synthesis gas and the lower inlet of the synthesis gas The port flow ratio is between 1/5-1/3, adjust the flow ratio of the upper air inlet and the lower air inlet to control the flow velocity of the syngas in the slurry so that the catalyst particles are evenly mixed in the slurry and in a suspended state;

3. Syngas undergoes Fischer-Tropsch synthesis reaction in the slurry bed reactor to generate gas products and liquid products;

4. The gaseous product is discharged through the top exhaust port of the slurry bed reactor, and the liquid product gradually accumulates in the slurry bed reactor;

5. When the slurry height reaches 2/3-3/4 of the reactor height, open the outlet valve of the solid-liquid separator pipeline, and under the action of the reactor pressure, the liquid product will be discharged from the reactor through the solid-liquid separator; When the slurry height in the reactor drops below 2/3 of the reactor height, close the outlet valve of the solid-liquid separator pipeline;

6. Open the valve of the high-pressure _N2 blowback port to make the pipeline pressure slightly higher than the pressure in the reactor, and purge the residual catalyst in the solid-liquid separator through N2 to make the catalyst particles enter the reactor slurry;

In the above process, cooling water enters from the inlet of the cooling coil and moves out from the outlet of the cooling coil, and the temperature in the reaction process of the reactor is adjusted through the cooling water;

7. After the reaction is completed, discharge the slurry from the slurry outlet.

In the step 1, the slurry height is located at 1/2 of the reactor height.

In the second step, the flow ratio of the upper inlet of the syngas to the lower inlet of the syngas is 1/4.

The beneficial effects of the present invention are as follows:

1) The slurry bed reactor of the present invention is provided with two gas distributors, the bottom gas distributor is a mesh-like structure, which allows the biomass synthesis gas to pass through the bottom gas distributor evenly, driven by the air flow, the slurry The catalyst particles in the slurry also flow and are suspended in the slurry; the catalyst particles on the upper part of the slurry will gradually settle due to gravity, which will easily cause the density of the catalyst particles in the slurry to be uneven; The gas distributor in the middle layer is set up. The gas distributor in the middle layer has a concentric ring structure, which can flow the catalyst particles falling in the slurry again. By controlling the flow rate of the upper and lower inlets of the syngas, the slurry of the syngas in the reactor can be adjusted. The flow state in the slurry makes the catalyst evenly distributed and suspended in the slurry, which promotes the heat transfer, mass transfer and reaction efficiency of the slurry bed reactor.

2) The present invention is equipped with a solid-liquid separator above the inside of the slurry bed reactor, which can directly separate the liquid product and catalyst particles in the slurry bed reactor. The grid structure of the solid-liquid separator is smaller than the catalyst particles, which can make Most of the catalyst is separated from the liquid product and returned to the reactor slurry. The catalyst powder broken due to collision in the slurry bed reactor is blown back into the reactor through high-pressure _N2 , which will not cause the catalyst powder to stay in the reactor. The solid-liquid separator leads to blockage of the solid-liquid separator, which improves the catalyst utilization rate and solid-liquid separation effect.

Description of drawings

Fig. 1 is the structural representation of slurry bed reactor of the present invention;

Fig. 2 is the structural representation of the solid-liquid separator in Fig. 1;

Fig. 3 is the bottom gas distributor in Fig. 1;

Fig. 4 is the middle layer gas distributor among Fig. 1;

Among them, 1. Slurry bed reactor shell, 2. Solid-liquid separator, 3. Catalyst feed inlet, 4. Syngas upper inlet, 5. Syngas lower inlet, 6. Bottom gas distributor ,7. Middle layer gas distributor, 8. Slurry outlet, 9. Cooling water inlet, 10. Cooling water outlet, 11. Top exhaust port, 12. Liquid outlet, 13. High pressure N2 blowback port, 14. Cooling plate Pipe, 21, spherical grid, 61, circular screen, 62, ceramic ring, 71, main air intake pipe, 72, air distribution holes.

Detailed ways

The present invention will be further described below in conjunction with the embodiments and accompanying drawings.

A slurry bed reaction device for preparing liquid fuel from biomass synthesis gas, comprising a slurry bed reactor shell 1, and a solid-liquid separator 2 is sequentially arranged in the slurry bed reactor shell 1 from top to bottom, The middle gas distributor 7 and the bottom gas distributor 6; the slurry bed reactor shell 1 is provided with a catalyst feed port 3 near the bottom end of the solid-liquid separator 2; the slurry bed reactor shell 1 is connected with the gas distributor 7 in the middle layer, and the upper end inlet port 4 of the synthesis gas is provided; the upper end of the slurry bed reactor shell 1 is provided with a top exhaust port 11, the bottom end is provided with a slurry discharge port 8, and the lower end is provided with a There is an air inlet 5 at the lower end of the synthesis gas; a cooling coil 14 is arranged in the slurry bed reactor shell 1, below the catalyst feed port 3, and above the bottom gas distributor 6; the cooling water of the cooling coil 14 Both the inlet 9 and the cooling water outlet 10 are located outside the slurry bed reactor shell 1, and the cooling water outlet 10 is located above the cooling water inlet 9; the solid-liquid separator 2 is provided with a liquid outlet pipe 12 communicating with the outside; A high-pressure N2 blowback port 13 is provided at the outlet end of the liquid outlet pipe 12 located outside the slurry bed reactor shell 1 .

The slurry bed reactor shell 1 includes a cylindrical body, and spherical caps are respectively arranged at the upper and lower ends of the cylindrical 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 made of a spherical mesh, and the spherical mesh The grid aperture is 0.1-0.2 um;

The middle layer gas distributor 7 is composed of several concentric ring pipes; each concentric ring is evenly distributed with air distribution holes 72 with openings facing upward; the middle layer gas distributor 7 is provided with concentric ring pipes. The cross-shaped main inlet pipe 71; the middle layer gas distributor 7 is located at 1/4-1/3 of the height of the slurry bed reactor;

The gas distributor 6 at the bottom layer is circular, including upper and lower layers of screens 61 and a purification layer between the upper and lower layers of circular screens 61; the aperture of the screens 61 is 0.2-0.5 um; the purification layer is filled with Equipped with a ceramic ring, the inner diameter of the ceramic ring is 1-3mm.

The bottom end of the solid-liquid separator is located at 2/3 of the height of the slurry bed reactor; the aperture of the spherical mesh is 0.1um;

The middle layer gas distributor 7 is located at 1/3 of the height of the slurry bed reactor.

The pore size of the screen 61 is 0.2 um, and the inner diameter of the ceramic ring is 2 mm.

The cooling water inlet 9 of the cooling coil 14 is close to the shell of the bottom distributor, and the cooling water outlet 10 is at 1/2 of the height of the slurry bed reactor.

A method for producing liquid fuel by using the above-mentioned biomass synthesis gas in a slurry bed reactor for Fischer-Tropsch synthesis, using a middle layer gas distributor and a bottom gas distributor to circulate the biomass synthesis gas to promote catalyst particles in the slurry Uniform distribution, using the cooling coil to remove the heat released by the Fischer-Tropsch synthesis reaction, using a solid-liquid separator to separate the liquid product from the catalytic particles in the slurry, and using high-pressure N to backflush the solid _- liquid separator to remove Catalyst particles remaining in the solid-liquid separator.

Including the following steps:

1. Open the upper cover of the slurry bed reactor shell, inject the slurry so that its height is at 1/2-2/3 of the reactor height, and close the upper cover;

Two, the biomass synthesis gas is divided into two streams of gas, which pass through the upper inlet 4 of the synthesis gas and the lower inlet 5 of the synthesis gas into the slurry bed reactor, the upper inlet 4 of the synthesis gas and the synthesis gas The flow ratio of the lower air inlet 5 is between 1/5-1/3, adjust the flow ratio of the upper air inlet and the lower air inlet to control the flow velocity of the syngas in the slurry so that the catalyst particles are evenly mixed in the slurry and in a state of suspended state;

3. Syngas undergoes Fischer-Tropsch synthesis reaction in the slurry bed reactor to generate gas products and liquid products;

4. The gaseous product is discharged through the outlet 11 on the top of the slurry bed reactor, and the liquid product gradually accumulates in the slurry bed reactor;

5. When the slurry height reaches 2/3-3/4 of the reactor height, open the outlet valve of the solid-liquid separator pipeline, and under the action of the reactor pressure, the liquid product will be discharged from the reactor through the solid-liquid separator; When the slurry height in the reactor drops below 2/3 of the reactor height, close the outlet valve of the solid-liquid separator pipeline;

6. Open the valve of the high-pressure _N2 blowback port to make the pipeline pressure slightly higher than the pressure in the reactor, and purge the residual catalyst in the solid-liquid separator through _N2 to make the catalyst particles enter the reactor slurry;

In the above process, cooling water enters from the inlet of the cooling coil and moves out from the outlet of the cooling coil, and the temperature in the reaction process of the reactor is adjusted through the cooling water;

7. After the reaction is completed, discharge the slurry from the slurry outlet.

In the step 1, the slurry height is located at 1/2 of the reactor height.

In the second step, the flow ratio of the upper inlet port 4 of the syngas to the lower inlet port 5 of the syngas is 1/4.

As shown in Figure 1, a slurry bed reaction device for producing liquid fuel from biomass synthesis gas consists of a slurry bed reactor shell 1, a solid-liquid separator 2, a cooling coil 14, a bottom gas distributor 6, a middle layer Gas distributor 7 and other parts; the main structure of the slurry bed reactor shell 1 is cylindrical, the upper and lower ends are spherical covers, a solid-liquid separator 2 is provided above the interior of the shell, and a middle gas layer is provided below the interior. The distributor 7 and the bottom gas distributor 6 are provided with a cooling coil 14 between the slurry inside the shell and the gas distributor.

The shell 1 of the slurry bed reactor is placed vertically, and the lower end is fixed by a base. Catalyst feed port 3 is provided on the upper side wall of the slurry bed reactor shell 1, and the feed port is located on the shell wall near the lower end of the solid-liquid separator, at 2/3-3/4 of the height of the slurry bed reactor place. The catalyst particles and liquid paraffin enter the slurry bed reactor through the catalyst feed port 3 after being uniformly mixed. The gas inlet 4 at the upper end of the synthesis gas is provided at the connection between the reactor shell and the gas distributor 7 in the middle layer, and the lower gas inlet 5 at the lower end of the synthesis gas is provided on the side wall of the lower spherical cover of the gas distributor 6 at the bottom layer, and the gas flow is controlled by a flow controller The flow rate of the material synthesis gas at the upper air inlet and the lower air inlet makes the flow ratio of the upper air inlet and the lower air inlet between 1/5-1/3, and in a preferred embodiment, the upper air inlet and the lower air inlet The air inlet flow ratio is 1/4. A top exhaust port 11 and a slurry discharge port 8 are respectively provided at the top and bottom of the slurry bed reactor shell, and the gas products generated by the Fischer-Tropsch synthesis reaction are discharged through the top exhaust port 11, and the gas products in the slurry bed reactor The slurry is discharged through the slurry discharge port 8 .

The solid-liquid separator 2 is located above the inside of the slurry bed reactor shell 1, and its bottom end is at 2/3-3/4 of the height of the slurry bed reactor. The solid-liquid separator has a cylindrical structure and is composed of spherical grids 21 with a grid aperture of 0.1-0.2um. In a preferred embodiment, the mesh diameter of the solid-liquid separator is 0.15 um, and its bottom end is located at 2/3 of the height of the slurry bed reactor.

A pipeline is connected to the top of the solid-liquid separator, and the pipeline leads to the outside of the slurry bed reactor. The pipeline is used for discharging the liquid product generated by the Fischer-Tropsch synthesis reaction in the reactor. A liquid outlet 12 is provided at the outlet of the pipeline, and a high-pressure N ₂ blowback port ₁₃ is provided at the outer end of the pipe, through which the catalyst particles remaining in the solid-liquid separator are blown back into the slurry bed reactor.

The middle layer gas distributor 7 is located in the middle and lower part of the shell of the slurry bed reactor, at 1/4-1/3 of the height of the reactor. The gas distributor in the middle layer is composed of distributor subunits with concentric ring structure, and air distribution holes 73 are evenly distributed on the arc-shaped distribution pipe 72 of each distributor subunit, and the openings of the gas distribution holes face upward. Biomass synthesis gas enters the slurry bed reactor through the stomata and flows upward. Main air intake pipes 71 are provided in four directions of the gas distributor in the middle layer for transporting biomass synthesis gas. In a preferred embodiment, the gas distributor in the middle layer is located at 1/3 of the height of the slurry bed reactor.

The bottom gas distributor 6 is located at the junction of the main structure of the slurry bed reactor and the lower end circular cover, and is a circular structure, divided into three layers, wherein the upper and lower layers are circular screens 61, the size of the screen aperture is 0.2-0.5 um, the middle layer is filled with ceramic rings 62, and the inner diameter of the ceramic rings is 1-3 mm. In a preferred embodiment, the pore size of the bottom gas distributor screen is 0.2 um, and the inner diameter of the ceramic ring is 2 mm.

Biomass synthesis gas is divided into two streams through the flow controller, and enters from the bottom gas distributor and the middle gas distributor respectively. The bottom gas distributor adopts a screen structure, which can evenly disperse the synthesis gas from the bottom into the reactor and drive the catalyst. Flow and disperse in slurry. The catalyst particles above the slurry will be deposited downward under the action of gravity, and the synthesis gas in the gas distributor in the middle layer flows out from above the gas distribution port, driving the catalyst to flow upward. By adjusting the flow controller, the flow rate of the biomass synthesis gas in the bottom gas distributor and the middle gas distributor is adjusted to promote the uniform distribution and suspension of the catalyst in the slurry bed reactor.

The cooling coil 14 is located between the slurry in the slurry bed reactor and the gas distributor, and the cooling coil is provided with a cooling water inlet 9 near the bottom gas distributor shell, at the height of the slurry bed reactor A cooling water outlet 10 is provided at 1/2. The excess heat released by the Fischer-Tropsch synthesis reaction is removed through the cooling coil to control the temperature of the reactor.

Catalyst particles and liquid paraffin are mixed evenly to form a slurry that enters the reactor through the feed port at the upper end of the slurry bed reactor, and the height of the slurry put into the reactor is at 1/2 - 2/3 of the height of the slurry bed reactor , In a preferred embodiment, the slurry height is set to 1/2 of the height of the slurry bed reactor.

The implementation method of the Fischer-Tropsch synthesis of the liquid fuel slurry bed reactor for preparing the biomass synthesis gas comprises using the slurry bed reactor to carry out the Fischer-Tropsch synthesis reaction, and using the middle layer gas distributor and the bottom gas distributor to carry out the Fischer-Tropsch synthesis. Biomass synthesis gas is circulated to promote the uniform distribution of catalyst particles in the slurry, the heat released by the Fischer-Tropsch synthesis reaction is removed by using the cooling coil, and the liquid product in the slurry is separated from the catalytic particles by a solid-liquid separator. Backflush the solid-liquid separator with high-pressure _N2 to remove the catalyst particles remaining in the solid-liquid separator.

The operation method of a slurry bed reactor for producing liquid fuel from biomass synthesis gas in the present invention also includes the following steps: 1) Divide the biomass synthesis gas into two streams, and control the flow rate of each stream of gas through a flow controller Flow rate, so that the flow ratio of the upper air inlet and the lower air inlet is between 1/5-1/3; 2) Synthesis gas enters the slurry inside the slurry bed reactor to drive the slurry flow, by adjusting the upper air inlet and the lower end The flow ratio of the gas inlet controls the velocity of the synthesis gas flowing in the reactor so that the catalyst particles are uniformly mixed in the slurry and in a suspended state; 3) The synthesis gas reacts with the catalyst in the slurry bed reactor to generate gas and liquid products ; 4) The gaseous product is discharged through the outlet at the top of the slurry bed reactor, and the liquid product gradually accumulates in the slurry bed reactor; 5) When the slurry height reaches 2/3 - 3/4 of the reactor height , open the outlet valve of the solid-liquid separator pipeline, under the action of the reactor pressure, the liquid product is discharged from the reactor through the solid-liquid separator, and the catalyst solid particles return to the slurry; 6) When the slurry height in the reactor drops to the reactor When the height is below 2/3, close the outlet valve of the solid-liquid separator pipeline; 7) Open the high-pressure N2 blowback valve to make the pipeline pressure slightly higher than the pressure in the reactor, and purge the residual catalyst in the solid-liquid separator with N2 , so that the catalyst powder is blown back into the reactor slurry; in the above process, the cooling water enters from the cooling coil inlet and moves out from the cooling coil outlet, and the temperature in the reaction process of the reactor is adjusted by the cooling water;

8) After the reaction is complete, discharge the slurry from the slurry outlet.

It should be understood that the parts not described in detail in this specification belong to the prior art.

It should be understood that the above-mentioned descriptions for the preferred embodiments are relatively detailed, and should not therefore be considered as limiting the scope of the patent protection of the present invention. Within the scope of protection, replacements or modifications can also be made, all of which fall within the protection scope of the present invention, and the scope of protection of the present invention should be based on the appended claims.

Claims (8)

1. A biomass synthesis gas production liquid fuel slurry bed reactor, characterized in that: comprising a slurry bed reactor shell (1), in the slurry bed reactor shell (1) from top to bottom A solid-liquid separator (2), a middle layer gas distributor (7) and a bottom gas distributor (6) are arranged in sequence at the bottom; on the slurry bed reactor shell (1), close to the solid-liquid separator (2) The bottom end is provided with a catalyst feed port (3); the joint of the slurry bed reactor shell (1) and the middle layer gas distributor (7) is provided with an air inlet (4) at the upper end of the synthesis gas; the slurry The top of the state bed reactor shell (1) is provided with a top exhaust port (11), the bottom end is provided with a slurry discharge port (8), and the lower end is provided with a synthesis gas lower end air inlet (5); the slurry state bed A cooling coil (14) is arranged in the reactor shell (1), below the catalyst feed inlet (3) and above the bottom gas distributor (6); the cooling water inlet (9) of the cooling coil (14) and the cooling water outlet (10) are all located outside the slurry bed reactor shell (1), and the cooling water outlet (10) is located above the cooling water inlet (9); the solid-liquid separator (2) is provided with A liquid outlet pipe (12) communicated with the outside world; the outlet end of the liquid outlet pipe (12) positioned outside the slurry bed reactor housing (1) is provided with a high _- pressure N blowback port (13); the solid-liquid The bottom end of the separator (2) is located at 2/3-3/4 of the height of the slurry bed reactor; the solid-liquid separator (2) is a sealed cylindrical structure made of a spherical mesh, and the spherical mesh The grid aperture is 0.1-0.2um; the middle layer gas distributor (7) is composed of several concentric ring pipes; each concentric ring is evenly distributed with openings facing upwards for air distribution holes (72); the middle layer gas The distributor (7) is provided with a cross-shaped main air inlet pipe (71) communicated with the concentric annular pipeline; the middle layer gas distributor (7) is located at 1/4-1/3 of the height of the slurry bed reactor; The bottom gas distributor (6) is circular and includes an upper and lower two-layer screen (61) and a purification layer between the upper and lower circular screens (61); the aperture of the screen (61) is 0.2 -0.5um; the purification layer is filled with ceramic rings, and the inner diameter of the ceramic rings is 1-3mm. 2. The slurry bed reaction device for preparing liquid fuel from biomass synthesis gas as claimed in claim 1, characterized in that: the slurry bed reactor shell (1) comprises a cylindrical main body, and the upper and lower sides of the cylindrical main body The ends are respectively provided with spherical caps. 3. the biomass synthesis gas preparation liquid fuel slurry bed reactor device as claimed in claim 1, is characterized in that: (1) 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 0.1um; (2) The middle layer gas distributor (7) is located at 1/3 of the height of the slurry bed reactor; (3) The aperture of the screen (61) is 0.2um, and the inner diameter of the ceramic ring is 2mm. 4. The biomass synthesis gas production liquid fuel slurry bed reaction device as claimed in claim 1, characterized in that: the cooling coil (14) cooling water inlet (9) is close to the shell of the bottom distributor, The cooling water outlet (10) is at 1/2 of the height of the slurry bed reactor. 5. A method utilizing the biomass synthesis gas described in any one of claims 1-4 to produce a liquid fuel slurry bed reactor to carry out Fischer-Tropsch synthesis, characterized in that: the middle gas distributor and the bottom gas distribution are utilized The device circulates the biomass synthesis gas to promote the uniform distribution of the catalyst particles in the slurry, uses the cooling coil to remove the heat released by the Fischer-Tropsch synthesis reaction, and uses the solid-liquid separator to separate the liquid product and the catalytic particles in the slurry. For separation, use high-pressure N to backflush the solid _- liquid separator to remove the catalyst particles remaining in the solid-liquid separator. 6. The method of claim 5, comprising the steps of: 1. Open the upper cover of the slurry bed reactor shell, inject the slurry so that its height is at 1/2-2/3 of the reactor height, and close the upper cover; 2. The biomass synthesis gas is divided into two streams of gas, which are respectively passed through the gas inlet (4) at the upper end of the synthesis gas, and the gas inlet (5) at the lower end of the synthesis gas is passed into the slurry bed reactor, and the gas inlet at the upper end of the synthesis gas is passed into the slurry bed reactor. (4), the flow ratio of the lower air inlet (5) of the synthesis gas is between 1/5-1/3, the flow ratio of the upper air inlet and the lower air inlet is adjusted to control the flow velocity of the synthesis gas in the slurry to make the catalyst Particles are uniformly mixed and suspended in the slurry; 3. Syngas undergoes Fischer-Tropsch synthesis reaction in the slurry bed reactor to generate gas products and liquid products; Four, the gaseous product is discharged through the outlet (11) at the top of the slurry bed reactor, and the liquid product gradually accumulates in the slurry bed reactor; 5. When the slurry height reaches 2/3-3/4 of the reactor height, open the outlet valve of the solid-liquid separator pipeline, and under the action of the reactor pressure, the liquid product will be discharged from the reactor through the solid-liquid separator; When the slurry height in the reactor drops below 2/3 of the reactor height, close the outlet valve of the solid-liquid separator pipeline; 6. Open the valve of the high-pressure _N2 blowback port to make the pipeline pressure slightly higher than the pressure in the reactor, and purge the residual catalyst in the solid-liquid separator through _N2 to make the catalyst particles enter the reactor slurry; In the above process, cooling water enters from the inlet of the cooling coil and moves out from the outlet of the cooling coil, and the temperature in the reaction process of the reactor is adjusted through the cooling water; 7. After the reaction is completed, discharge the slurry from the slurry outlet. 7. The method according to claim 6, characterized in that the slurry height in the step 1 is at 1/2 of the reactor height. 8. The method according to claim 6, characterized in that, in the step 2, the flow ratio of the upper inlet port (4) of the synthesis gas to the lower inlet port (5) of the synthesis gas is 1/4.