Production device for preparing biomass fuel from straw

Abstract

A production device for preparing biomass fuel from straw comprises a solvent storage tank (1), a first delivery pump (4), a first heater (5), a first reaction tank (6), a first gas-liquid separation tank (7) and a first oil storage tank (8) which are communicated through a pipeline, the bottom of the first oil storage tank (8) is communicated with a first oil delivery pipe (9), and a second delivery pump (10) and a second heater (11) are installed on the first oil delivery pipe (9). One end of the first oil conveying pipe (9) is communicated with a dehydration reaction tank (12), one end of the dehydration reaction tank (12) is sequentially communicated with a second gas-liquid separation tank (13) and a solvent recovery tank (14) through a pipeline, and the solvent recovery tank (14) is further communicated with a solvent recovery pipe (15) and a dehydration liquefaction oil conveying pipe (16). The device is simple in structure and convenient to use, the ash content in the bio-oil is reduced, the production efficiency and quality of the bio-oil are improved, and the production cost is reduced.

Description

Technical Field

[0001] The utility model relates to the field of bio-oil production, in particular to a production device for making biomass fuel from straw. Background Art

[0002] In the existing field of manufacturing liquefied fuel oil using biomass as raw material, the temperature during preparation and the use of catalysts affect the oil yield. For example: 1) water containing potassium carbonate as a biomass liquefaction catalyst and wood powder as a biomass raw material are treated at 200℃ to 385℃ to produce liquefied fuel oil with a solid content of 23% to 45% by weight relative to the biomass raw material;

[0003] 2) treating wood powder, water, neutral oxygen-containing solvent (acetone, methyl ethyl ketone, ethyl acetate, 1-butanol, etc.) and potassium carbonate at 300° C. to obtain liquefied fuel oil having a weight percentage of 33% to 68% relative to the solid content of the biomass raw material;

[0004] 3) treating wood powder, water, phenolic compounds (phenol, cresol) and alkali metal compounds or alkaline earth metal compounds (potassium carbonate, sodium carbonate, calcium carbonate, sodium hydroxide, calcium hydroxide, etc.) at 350° C. to obtain liquefied fuel oil having a weight percentage of 33% to 68% relative to the solid content of the biomass raw material;

[0005] 4) Treating lignocellulosic biomass with supercritical alcohol (methanol, etc.) at 320°C to 360°C to obtain liquefied fuel oil soluble in alcohol at a content of about 70% by weight relative to the solid content of the biomass;

[0006] 5) Treating woody biomass with a mixed solution of polyethylene glycol / glycerol / sulfuric acid = 70 / 30 / 3 (170° C. to 200° C.) to obtain liquefied fuel oil in an amount of 45% by weight based on the solid content of the biomass.

[0007] However, there are some problems in the above production: for example, in 1), since only water is used as the solvent for liquefaction, the liquefaction of water-insoluble lignin is insufficient, and the yield of liquefied fuel oil relative to the solid content of biomass is reduced. In addition, since potassium carbonate is used as a liquefaction catalyst, there is also a problem of ash remaining in the liquefied fuel oil; in 2), 5 parts of water and 1 part of a neutral oxygen-containing solvent are used as solvents for liquefaction, and the liquefaction of water-insoluble lignin is improved. However, the effect is not sufficient, and the yield of liquefied fuel oil relative to the solid content of biomass is not greatly improved. In addition, similar to 1), since an inorganic alkaline substance is used as a liquefaction catalyst, there is also a problem of ash remaining in the liquefied fuel oil; 3) By using a mixed solvent of water / phenolic compound = 5 / 1 to 1 / 1 as a solvent, the liquefaction of water-insoluble lignin is improved, but the effect is not sufficient, and the yield of liquefied fuel oil relative to the solid content of biomass is not much improved. As with 1) and 2), since an inorganic alkaline substance is used as a liquefaction catalyst, there is also a problem that it remains as ash in the liquefied fuel oil;

[0008] 4) Using supercritical alcohol (methanol, etc.) as a solvent, the yield of liquefied fuel oil relative to the solid content of biomass can be increased to 70% by weight. However, the liquefaction pressure of biomass is 43 MPa, which is very high, and there is a problem that the liquefaction reaction equipment becomes expensive;

[0009] 5) Using a mixed solution of polyethylene glycol / glycerol / sulfuric acid = 70 / 3 as a solvent, the yield of liquefied fuel oil relative to the biomass solid content was increased to 90% by weight. However, since sulfuric acid is used as an acid catalyst, high-grade materials such as nickel alloy must be used in the material of the liquefaction reaction device, which has the problem of making the cost of the entire device very expensive.

[0010] In addition, the above-mentioned existing production equipments all have the problem of complex equipment structure and high unit price, which makes the production cost high. Utility Model Content

[0011] The utility model aims to overcome the shortcomings of the prior art and provide a production device for biomass fuel made from straw, which can improve the production efficiency of liquefied fuel oil and reduce the ash residue.

[0012] This application provides the following technical solutions:

[0013] A production device for biomass fuel made from straw, characterized in that it comprises a solvent storage tank, a first delivery pump, a first heater, a first reaction tank, a first gas-liquid separation tank, and a first oil storage tank which are connected at one time through a pipeline; a first oil pipeline is connected at the bottom of the first oil storage tank; a second delivery pump and a second heater are sequentially installed on the first oil pipeline; a dehydration reaction tank is connected at one end of the first oil pipeline; a second gas-liquid separation tank and a solvent recovery tank are sequentially connected at one end of the dehydration reaction tank through a pipeline; a solvent recovery pipe and a dehydration liquefaction oil pipeline are also connected to the solvent recovery tank; a biomass raw material layer is placed in the first reaction tank, and a dehydration catalyst is placed in the dehydration reaction tank.

[0014] On the basis of the above technical solutions, there are also the following further technical solutions:

[0015] A liquid mixing device is provided on the pipeline between the first delivery pump and the solvent storage tank, the liquid mixing device is connected with a water supply pipe, and a corresponding matching flow control valve is provided on the water supply pipe.

[0016] The solvent in the solvent storage tank does not contain any of an acid catalyst and a base catalyst.

[0017] The solvent in the solvent storage tank contains an organic solvent having 3 to 12 carbon atoms.

[0018] The solvent in the solvent storage tank contains an aromatic hydrocarbon solvent as an organic solvent.

[0019] The aromatic hydrocarbon solvent is xylene or 1-butanol solvent.

[0020] The liquid mixing device comprises a shell, in which a vertically distributed orifice plate is arranged, and on the inner wall of the shell on one side of the orifice plate a spiral is arranged along the axial direction thereof, thereby forming a spiral liquid mixing channel.

[0021] A first orifice plate is provided in the first reaction tank at the upper end of the biomass raw material layer, and a second orifice plate is provided in the first reaction tank at the lower end of the biomass raw material layer.

[0022] The biomass raw material layer is a biomass raw material containing wood cellulose that is crushed into a diameter of less than 1 mm and a water content of 5-20% by weight.

[0023] Advantages of utility models:

[0024] The utility model has a simple structure and is easy to use. It can well maintain the balance between the liquefaction of water-insoluble lignin and the liquefaction of water-soluble cellulose, improve the production efficiency of biomass liquefied fuel oil, i.e., bio-oil, and reduce the ash content of bio-oil, thereby improving the quality of biomass fuel. In addition, aromatic hydrocarbon solvents can be recovered for reuse. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 It is a schematic diagram of the structure of Embodiment 1 of the present utility model;

[0026] Figure 2 It is a schematic structural diagram of the liquid mixing device 3 in Example 2. DETAILED DESCRIPTION

[0027] Example 1

[0028] like Figure 1 As shown, a production device for straw-based biomass fuel includes a solvent storage tank 1, a first delivery pump 4, a first heater 5, a first reaction tank 6, and a first gas-liquid separation tank 7 which are sequentially connected through pipelines.

[0029] The solvent in the solvent storage tank 1 does not contain any of an acid catalyst and an alkali catalyst, and contains an organic solvent having 3 to 12 carbon atoms, wherein the organic solvent contains an aromatic hydrocarbon solvent, ie, xylene solvent.

[0030] An electric heating device 6c is sleeved on the outer wall of the first reaction tank 6, a horizontally distributed first orifice plate 6a is connected to the upper end of the inner wall of the first reaction tank 6, and a horizontally distributed second orifice plate 6b is connected to the lower end of the first reaction tank 6. The space between the first orifice plate 6a and the second orifice plate 6b is filled with a biomass raw material layer 17 (such as straw or corn stalks) containing lignocellulose that is crushed to a diameter of less than 1 mm and a moisture content of 15% by weight. The straw used in this embodiment.

[0031] An exhaust pipe 19 is connected to the top of the first gas-liquid separation tank 7, on which a corresponding gas pipe control valve 19a is installed. One side of the first gas-liquid separation tank 7 is connected to the first oil storage tank 8 through a pipeline, and a corresponding oil discharge valve 8a is installed on the pipeline.

[0032] A first oil pipeline 9 is connected to the bottom of the first oil storage tank 8, and a second delivery pump 10 and a second heater 11 are installed in sequence on the first oil pipeline 9. A dehydration reaction tank 12 is connected to one end of the first oil pipeline 9. The structure of the dehydration reaction tank 12 is the same as that of the first reaction tank 6 and its structure is not repeated here. The difference between the two is that a dehydration catalyst 18 is placed between the two layers of perforated plates in the dehydration reaction tank 12.

[0033] The dehydration catalyst 18 is not particularly limited to any catalyst that promotes the dehydration reaction, and may be a catalyst of metal oxides such as silicate (silicate), alumina, aluminum silicate (zeolite), and titanium dioxide.

[0034] A second gas-liquid separation tank 13 is provided at one end of the dehydration reaction tank 12 through a pipeline. A second exhaust pipe 13a is provided on the top of the second gas-liquid separation tank 13, and a corresponding gas pipe control valve 13b is installed on the second exhaust pipe 13a.

[0035] The bottom of the second gas-liquid separation tank 13 is connected to a solvent recovery tank 14 through a pipeline, the top of the solvent recovery tank 14 is connected to a solvent recovery pipe 15, and the bottom of the second gas-liquid separation tank 13 is connected to a dehydration liquefaction oil pipeline 16.

[0036] Working process:

[0037] A lignocellulosic biomass raw material with a moisture content of about 10% by weight is filled into the first reaction tank 6, and xylene solvent is used. The solvent is heated by a first heater from the time the temperature is raised to 300°C and circulated in the first reaction tank for 1 hour to carry out the liquefaction treatment of the biomass. During the whole process, the moisture content of the biomass raw material layer in the first reaction tank is ensured to be within 15%-20% by weight, and the reaction pressure during the liquefaction treatment is adjusted to 12MPaG.

[0038] When the water content of the biomass raw material layer is excessive during the entire reaction, the decomposition of cellulose or hemicellulose is promoted, but the decomposition products are dissolved in the water phase only at a low concentration, resulting in a problem that the yield of liquefied fuel oil cannot be obtained.

[0039] The liquefied biomass fuel oil and gas generated after the reaction in the first reaction tank enter the first gas-liquid separation tank for gas-liquid separation, and then the biomass fuel oil enters the first oil storage tank. At this time, the biomass fuel oil contains aromatic hydrocarbon solvents and excessive water. After passing through the second delivery pump and the second heater, the biomass fuel oil reaching the dehydration reaction temperature enters the dehydration reaction tank for dehydration. Since the temperature and dehydrating agent used in the dehydration reaction are both existing technologies, they will not be described here.

[0040] After the dehydration reaction, the dehydrated liquefied biomass fuel oil and the generated gas are separated again by gas-liquid separation in the second gas-liquid separation tank 13, and finally enter the solvent recovery tank 14 to separate the aromatic hydrocarbons and the dehydrated liquefied fuel oil. The specific separation method is also an existing method such as distillation. The separated solvent is recovered through the solvent recovery pipe, and the dehydrated liquefied fuel oil flows out through the dehydrated liquefied oil pipeline 16. Example 2

[0041] like Figure 2 As shown, the difference between Example 2 and Example 1 is that a liquid mixing device 3 is installed on the pipeline between the solvent storage tank and the first delivery pump 4, the liquid mixing device 3 is connected to a water supply pipe 2, and a corresponding matching flow control valve 2a is provided on the water supply pipe 2.

[0042] This is because when the water content of the biomass raw material is low, it needs to be replenished with water, and it is also necessary to consider that the replenished water and the organic solvent in the solvent storage tank 1 are fully mixed before entering the first reaction tank. Because the water content of the material during the reaction in the first reaction tank is 10% to 25% (if 1-butanol solvent is used, the water content of the material during the reaction in the first reaction tank is 15% to 25%). Otherwise, the production efficiency of biomass fuel oil will be affected.

[0043] The liquid mixing device 3 comprises a shell 3a, in which a vertically distributed orifice plate 3d is arranged, and on the inner wall of the shell 3a on one side of the orifice plate 3d, a spiral is arranged along the axial direction thereof, thereby forming a spiral liquid mixing channel 3e.

[0044] The xylene solvent or 1-butanol solvent and water are fully dispersed through the orifice plate, and then the fully mixed inlet solvent and the replenishing water are mixed through the spiral mixing channel.

Claims

1. A production device for straw-based biomass fuel, characterized in that: The invention comprises a solvent storage tank (1), a first delivery pump (4), a first heater (5), a first reaction tank (6), a first gas-liquid separation tank (7), and a first oil storage tank (8) which are connected in sequence through pipelines; a first oil delivery pipe (9) is connected at the bottom of the first oil storage tank (8); a second delivery pump (10) and a second heater (11) are installed in sequence on the first oil delivery pipe (9); a dehydration reaction tank (12) is connected at one end of the first oil delivery pipe (9); a second gas-liquid separation tank (13) and a solvent recovery tank (14) are connected in sequence at one end of the dehydration reaction tank (12) through pipelines; a solvent recovery pipe (15) and a dehydration liquefaction oil delivery pipe (16) are also connected to the solvent recovery tank (14); a biomass raw material layer (17) is placed in the first reaction tank (6); and a dehydration catalyst (18) is placed in the dehydration reaction tank (12).

2. The production device of straw-based biomass fuel according to claim 1, characterized in that: A liquid mixing device (3) is provided on the pipeline between the first delivery pump (4) and the solvent storage tank (1), a water supply pipe (2) is connected to the liquid mixing device (3), and a corresponding matching flow control valve (2a) is provided on the water supply pipe (2).

3. The production device of straw-based biomass fuel according to claim 1, characterized in that: The solvent in the solvent storage tank (1) does not contain any of an acid catalyst and a base catalyst.

4. The production device of straw-based biomass fuel according to claim 1, characterized in that: The solvent in the solvent storage tank (1) contains an organic solvent having 3 to 12 carbon atoms.

5. The production device of straw-based biomass fuel according to claim 1, characterized in that: The solvent in the solvent storage tank (1) contains an aromatic hydrocarbon solvent as an organic solvent.

6. The production device of straw-based biomass fuel according to claim 5, characterized in that: The aromatic hydrocarbon solvent is xylene or 1-butanol.

7. The production device of straw-based biomass fuel according to claim 2, characterized in that: The liquid mixing device (3) comprises a shell (3a), wherein a vertically distributed orifice plate (3d) is provided in the shell (3a), and a spiral extending along the axial direction is provided on the inner wall of the shell (3a) on one side of the orifice plate (3d), thereby forming a spiral liquid mixing channel (3e).

8. The production device of straw-based biomass fuel according to claim 1, characterized in that: A first orifice plate (6a) is provided in the first reaction tank (6) at the upper end of the biomass raw material layer (17), and a second orifice plate (6b) is provided in the first reaction tank (6) at the lower end of the biomass raw material layer (17).

9. The production device of straw-based biomass fuel according to claim 1, characterized in that: The biomass raw material layer (17) is a biomass raw material containing lignocellulose that is crushed into a diameter of less than 1 mm and has a moisture content of 5-20% by weight.

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