Fluidized bed coupling treatment method for solid-containing slurry and device for implementing method

Abstract

The invention relates to a fluidized bed coupling treatment method for solid-containing slurry and a device for implementing the method, and the method comprises the following steps: two solid-containing slurry with different properties are respectively subjected to fluidization pyrolytic reaction in two fluidized bed reactors, and generated products respectively enter respective fractionating towers; the heat of the two reactors is provided by the two charring tanks, and the side with excessive heat supplies heat to the side with insufficient heat, so that the overall heat balance is realized. The coupling treatment of the two kinds of solid-containing slurry can realize the advantage complementation of the two kinds of raw materials, the overall heat balance of the device is realized, solids in the raw materials are recovered, and the overall oil yield is improved.

Description

Technical Field

[0001] The present invention belongs to the field of coal chemical industry and petrochemical industry, and in particular, relates to a fluidized bed coupling treatment method for solid slurry and a device for implementing the method. Background Art

[0002] A large amount of industrial solid-containing slurries are generated during the chemical production process in the coal chemical and petrochemical fields. The common characteristics of these slurries are that they are composed of solids and organic matter. They are solid, liquid or asphalt-like at room temperature. Their solid content and organic matter composition vary with the processing raw materials and processes. For example, the solids in the slurry may be metals contained in the crude oil itself, or they may be catalysts added during the coal liquefaction process or unreacted coal and ash; the organic matter may be high-boiling point long-chain hydrocarbons or heavy oil produced by the Fischer-Tropsch synthesis reaction, or it may be asphaltene, pre-asphaltene or high-boiling point distillate oil produced during the petroleum refining process. This type of slurry has the characteristics of solid content, high viscosity, high boiling point, and low value. Its conversion and utilization has always been an industrial problem.

[0003] In the process of indirect coal liquefaction, the slurry bed reactor needs to regularly replace the catalyst and filter and purify the Fischer-Tropsch heavy wax. These operations will produce a large amount of solid slurry containing catalyst particles and filter media (solid content of 5wt% to 60wt%), which contains a certain amount of heavy wax. If it is not recycled, it will cause oil loss. The Fischer-Tropsch solid slag wax is currently mainly treated by incineration, and the distillate oil cannot be recycled, which causes a waste of carbon resources to a certain extent and also causes a large amount of CO 2 Emissions. The coking of coal or the fixed-bed gasification of coal will produce some solid or dusty coal tar, which also needs to be processed and utilized more efficiently.

[0004] In the oil refining industry, for petroleum-based atmospheric residue or vacuum residue with very low solid content (0.1-5wt%) but relatively high Conradson carbon value, thermal conversion process methods such as delayed coking can usually be used for treatment. However, delayed coking is an intermittent operation, which requires regular furnace turnover, conversion and coke cleaning operations. It is an intermittent operation device and has certain safety risks. The outlet of the large amount of sulfur-containing petroleum coke produced has gradually become a problem, and the coking rate during the reaction process is high. A continuous and pollution-free technology is urgently needed to replace it. FCC tail oil slurry, solid-containing shale oil, oil sand asphalt, etc. in the oil refining industry are also solid-containing slurries, which require appropriate conversion and processing technology. The heavy oil or atmospheric and vacuum residue suspended bed / slurry bed hydrogenation process in the oil refining process will also produce some solid-containing atmospheric and vacuum residues, which require appropriate treatment solutions.

[0005] For chemical wastewater treatment plants, biochemical pools regularly discharge large amounts of activated sludge, and the large amounts of carbon-containing organic matter resources contained in these sludges also need to be recycled.

[0006] As can be seen from the above, a large amount of industrial solid-containing slurry will be produced in the fields of coal chemical industry and petrochemical industry. There is an urgent need for an efficient, continuous and environmentally friendly processing technology to achieve maximum resource recovery and utilization of solids while converting and utilizing oil products at a high yield.

[0007] The fluidized bed conversion of the above raw materials may have the following problems due to the differences in the properties of the raw materials:

[0008] 1) Raw materials with high coking rate usually have abundant heat, and some coke particles need to be discharged to maintain heat balance. However, the treatment of the discharged coke particles is a difficult problem, which usually requires supporting gasification or boiler coking process.

[0009] 2) Raw materials with low coking rate usually lack sufficient heat to meet the process heat balance and require additional fuel.

[0010] 3) When the solid content of the solid slurry is high, it is necessary to continuously discharge the solid particles. If these particles cannot be completely burned, a layer of coke will be attached to the solid particles, which is not conducive to the treatment of the solid and brings new solid waste problems. At the same time, part of the coke is wasted, causing heat imbalance in the system.

[0011] 4) Some raw materials contain a large amount of fine powder, which can easily enter the oil and gas system, causing difficulties in handling heavy oil and dust.

[0012] In view of the characteristics of various solid-containing slurries of different properties, the present invention proposes a fluidized bed coupling treatment process and device for solid-containing slurries, which can achieve complementary advantages of different raw materials and improve the overall energy conversion efficiency and process economy. Summary of the invention

[0013] The inventors have discovered through research that coupling two solid-containing slurries with different coking rates in the same device can solve the problems existing in the separate treatment of the two raw materials, making it easier for the device to achieve heat balance, and obtain a higher oil yield, thereby achieving effective recovery and utilization of solids.

[0014] The raw materials of the present invention are divided into two types. Raw material A is a solid-containing slurry with a high coking rate and a low solid content, such as coal tar / refinery vacuum residue oil, etc., and raw material B is a solid-containing slurry with a low coking rate and a high solid content. Raw material A has abundant heat when subjected to fluidized pyrolysis alone, and some coke particles need to be extracted. Raw material B has insufficient heat when subjected to fluidized pyrolysis alone, and external fuel needs to be introduced to supplement heat. Raw material A has a low solid content, is liquid or slurry at room temperature, and is liquid after heating, so liquid feed can be used. Raw material B has a high solid content, is solid at room temperature, and can be fed in a solid state. The properties of the two raw materials are quite different, and the properties of the generated oil products are also different, so they are more valuable when processed separately. If the oil product generated by raw material B is a clean sulfur-free and nitrogen-free Fischer-Tropsch hydrocarbon distillate oil, its value will be reduced if tar with a high impurity content is mixed in.

[0015] Therefore, a first aspect of the present invention is to provide a fluidized bed coupling treatment method for solid-containing slurry, the method comprising:

[0016] After raw material A is mixed with the high-temperature solid-containing slurry from the bottom of the first distillation tower 6 in the raw material mixing tank 10, it enters the first fluidized pyrolysis reactor A1 after being atomized by the nozzle feeding system, undergoes pyrolysis reaction, generates high-temperature oil gas and coke, and the high-temperature oil gas is discharged from the top of the reactor and enters the first distillation tower 6 to generate top products and high-temperature solid-containing slurry from the bottom of the tower, and the coke is transported to the oxygen-depleted combustion tank 2; raw material B enters the second fluidized pyrolysis reactor A2 through the solid feeding device 3, undergoes pyrolysis reaction, generates high-temperature oil gas and coke, and the high-temperature oil gas It is discharged from the top of the reactor and enters the second distillation tower 7 to generate a tower top product and a tower bottom oil slurry; the tower top products of the two oil and gas distillation towers are respectively sent to the downstream processing device; wherein, both raw materials A and B are solid slurries, the solid content of raw material A is less than that of raw material B, and the coking rate of raw material A is higher than that of raw material B; the heat required by the first fluidized pyrolysis reactor A1 is provided by the oxygen-depleted combustion tank 2 through the circulation of coke particles; the heat required by the second fluidized pyrolysis reactor A2 is provided by the oxygen-rich combustion tank 4 through the circulation of solid heat carriers.

[0017] In one embodiment, the heat required by the first fluidized pyrolysis reactor A1 is provided by the oxygen-depleted combustion tank 2 through the circulation of coke particles. The high-temperature carbon particles from the oxygen-depleted combustion tank 2 contact the raw materials in the fluidized pyrolysis reactor A1, provide the required reaction heat, and further undergo a pyrolysis reaction. The particle size becomes larger and is discharged from the bottom of the reactor and enters the oxygen-depleted combustion tank 2. In the oxygen-depleted burner 2, the coke undergoes an oxidation reaction with oxygen, the particle size is reduced, a part of it is circulated back to the first fluidized pyrolysis reactor A1, and the remaining part enters the oxygen-enriched combustion tank 4 for a complete coke combustion reaction. After the reaction, only inorganic ash particles remain. Preferably, the inorganic ash particles are discharged from the system together with the solid inorganic matter in the second fluidized pyrolysis reactor A2 through a solid discharge line.

[0018] In one embodiment, the heat required by the second fluidized pyrolysis reactor A2 is provided by the oxygen-enriched combustion tank 4 through the circulation of solid heat carrier. After the high-temperature heat carrier from the oxygen-enriched combustion tank 4 enters the second fluidized pyrolysis reactor A2, it contacts with the raw material to cause a thermal cracking reaction of the raw material. A small amount of coke is attached to the heat carrier and returned to the oxygen-enriched combustion tank 4. In the oxygen-enriched combustion tank 4, the heat carrier with a small amount of coke attached and the coke from the oxygen-depleted combustion tank 2 contact with oxygen to react with combustion, generating a large amount of heat, and all the coke is converted into CO 2 The temperature of the heat carrier in the gas increases, and a part of it is circulated back to the second fluidized pyrolysis reactor A2, and the excess heat carrier is discharged from the oxygen-enriched combustion tank 4, and discharged from the system after the heat is recovered.

[0019] In one embodiment, the high-temperature flue gas at the top of the oxygen-rich combustion tank 4 enters the oxygen-lean combustion tank 2 to supplement heat for the oxygen-lean combustion tank 2, and then returns from the oxygen-lean combustion tank 2 to the middle of the first fluidized pyrolysis reactor A1, and then returns from the oxygen-rich combustion tank 4 to the middle of the second fluidized pyrolysis reactor A2.

[0020] In one embodiment, the high-temperature flue gas at the top of the oxygen-rich combustion tank 4 enters the oxygen-depleted combustion tank 2 to supplement the heat for the oxygen-depleted combustion tank 2, and finally enters the flue gas washing treatment device together with the tail gas of the oxygen-depleted combustion tank 2. In order to achieve the stability of the particle size distribution of the solid particles in the oxygen-depleted burner 2, it is necessary to add a small amount of high-temperature heat carrier from the oxygen-rich combustion tank 4 into the oxygen-depleted combustion tank 2.

[0021] In one embodiment, the solid heat carrier may be a carrier such as quartz sand at the time of start-up, and is gradually replaced by the solid inorganic matter generated in the second fluidized pyrolysis reactor A2 as the reaction proceeds.

[0022] In one embodiment, the solid content of raw material A is 1-25%, and the coking rate is 2-30%. Preferably, raw material A can be selected from coal tar, vacuum residue oil from refinery, and the like.

[0023] In one embodiment, the ratio of the raw material A to the high-temperature solid slurry at the bottom of the first fractionation tower is 70-99:1-30, preferably, the ratio is 80-98:2-20.

[0024] In one embodiment, the solid content of raw material B is 5-55 wt %, and the coking rate is 0-5 wt %. Preferably, raw material B can be selected from slag wax, for example, indirectly liquefied slag wax.

[0025] In one embodiment, the first fluidized pyrolysis reactor A1 undergoes thermal cracking and condensation reactions at a temperature of 500-600°C, a pressure of 0.1-0.25 MPa, and an empty gas velocity of 0.45-1.0 m / s to obtain high-temperature oil and gas, coke, and solid inorganic matter.

[0026] In one embodiment, the second fluidized pyrolysis reactor A2 undergoes thermal cracking and a very small amount of condensation reaction at a temperature of 500-580°C, a pressure of 0.1-0.25 MPag, and an empty gas velocity of 0.55-0.8 m / s to obtain high-temperature oil and gas, coke, and solid inorganic matter.

[0027] In one embodiment, in order to prevent the accumulation of solid fine powder in the slurry at the bottom of the first fluidized bed reactor A1, a small amount of solid slurry at the bottom of the tower can be transported into the oxygen-depleted combustion tank 2 for combustion to supplement the system heat, and the fine powder is discharged from the top of the oxygen-depleted combustion tank 2. In the first fluidized bed reactor A1, due to the high coking rate of the raw material, the fine powder particles can serve as the coking center, and the coking layers on the surface of the particles gradually grow, and the generated coke particles enter the oxygen-depleted combustion tank.

[0028] In one embodiment, the fine powder discharged from the top of the oxygen-poor combustion tank 2 is collected and discharged via a cyclone separator 5 .

[0029] In one embodiment, the heat required by the first fluidized pyrolysis reactor is provided by the oxygen-depleted combustion tank 2 through the coke circulation of 2000-8000 kg / hr, and the heat required by the second fluidized pyrolysis reactor is provided by the oxygen-rich combustion tank 4 through the carrier circulation of 2000-6000 kg / hr.

[0030] The second aspect of the present invention is to provide a fluidized bed coupling processing equipment for solid slurry, which includes: a first fluidized pyrolysis reactor A1, a second fluidized pyrolysis reactor A2, an oxygen-depleted combustion tank 2, an oxygen-rich combustion tank 4, a first distillation tower 6, a second distillation tower 7, a solid feeding device 3, and a raw material mixing tank 10.

[0031] In one embodiment, the top outlet of the first fluidized pyrolysis reactor A1 is connected to the raw material inlet of the first fractionation tower 6, and the top outlet of the second fluidized pyrolysis reactor A2 is connected to the raw material inlet of the second fractionation tower 7. The raw material mixing tank 10 is used to mix the raw material A and the high-temperature solid-containing slurry at the bottom of the first fractionation tower 6, and its outlet is connected to the raw material inlet of the first fluidized pyrolysis reactor A1; the first fluidized pyrolysis reactor A1 is used to pyrolyze the raw material A into high-temperature oil and gas and coke, and the high-temperature oil and gas enter the first fractionation tower 6, and the coke is transported to the oxygen-depleted combustion tank 2; the second fluidized pyrolysis reactor A2 is used to pyrolyze the raw material B into high-temperature oil and gas and coke, and the high-temperature oil and gas enter the second fractionation tower 7.

[0032] In one embodiment, Raw Material A and Raw Material B are as described herein above.

[0033] In one embodiment, the heat required by the first fluidized pyrolysis reactor A1 is provided by the oxygen-depleted combustion tank 2 through the char particle circulation, and the heat required by the second fluidized pyrolysis reactor A2 is provided by the oxygen-rich combustion tank 4 through the solid heat carrier circulation.

[0034] In one embodiment, the high-temperature flue gas at the top of the oxygen-rich combustion tank 4 enters the oxygen-lean combustion tank 2 to supplement the heat for the oxygen-lean combustion tank 2 .

[0035] In one embodiment, the device further comprises a cyclone separator 5 , which is connected to the top of the oxygen-lean burner 2 and is used to collect and discharge fine powder in the oxygen-lean combustion tank 2 .

[0036] The features and advantages of the present invention are as follows:

[0037] 1) Raw material A has a low solid content and a high coke rate. It is fed in a highly dispersed liquid phase and undergoes a pyrolysis reaction in a separate fluidized bed reactor. The reaction parameters such as reaction temperature and residence time are adjusted according to the reaction characteristics to increase the oil yield and reduce the risk of coke blockage in the reactor.

[0038] 2) Raw material B has a high solid content and a low coke yield. It can be fed in the solid phase and undergo pyrolysis in a separate fluidized bed reactor. Reaction parameters such as reaction temperature and residence time are adjusted according to the reaction characteristics to improve the oil yield.

[0039] 3) The heat of the first fluidized bed reactor A1 is provided by the oxygen-poor burner, and the heat transfer between the two devices is achieved by the circulation of coke particles. The temperature of the oxygen-poor coke burning tank is relatively low, part of the heat is provided by the flue gas of the oxygen-rich coke burning tank, and the other part is provided by the coking reaction of oxygen and coke. Controlling the oxygen concentration can achieve the temperature regulation of coke particles. The flue gas outlet temperature of the oxygen-poor coke burning tank is low, and the oxygen content is low, which reduces the overall air consumption of the entire system and reduces energy consumption.

[0040] 4) The heat of the second fluidized bed reactor A2 is provided by the oxygen-rich burner, and the heat transfer between the two devices is achieved by the circulation of solid heat carrier particles. The solid heat carrier can be a carrier such as quartz sand when starting up, and is gradually replaced by solid particles in raw material B as the reaction proceeds. There is an excess of oxygen in the oxygen-rich burner, and a higher temperature can be used to completely burn the organic matter on the coke particles from the oxygen-poor burner to provide heat for the solid heat carrier. The solid heat carrier does not contain organic matter such as coke, and will not introduce pollutants such as sulfur and nitrogen into the second fluidized bed reactor A2, ensuring the cleanliness of the reactor product and avoiding contamination of oil products by coke impurities. The high-temperature flue gas from the oxygen-rich burner is further heat exchanged and cooled in the oxygen-poor burner, and the unreacted oxygen is further reacted, which can improve the oxygen utilization rate and thermal energy utilization rate.

[0041] 5) A part of the solid particles entrained in the two raw materials are discharged from the oxygen-enriched burner discharge system, and a small amount of fine powder is finally discharged from the top of the oxygen-depleted burner after being collected by the cyclone separator. The solid particles discharged from the oxygen-enriched burner do not contain organic matter and do not require subsequent treatment procedures, which can achieve resource utilization of solids. The small amount of fine powder discharged from the cyclone separator may contain coke, which can be incinerated.

[0042] The present invention realizes the fluidized bed coupling treatment of two solid-containing raw materials of different properties, which not only realizes heat balance, improves process energy efficiency and oil yield, and ensures the quality of oil products in the two raw materials, but also the discharged solids do not contain organic matter, which is easy to be recycled and realizes the resource utilization of solids. The device is continuously operated, does not require external heating, is safe and environmentally friendly, and has a good application prospect. BRIEF DESCRIPTION OF THE DRAWINGS

[0043] Figure 1 Schematic diagram of an exemplary device for implementing a fluidized bed coupling treatment method for two different solid-containing slurries. In which, each reference numeral represents:

[0044] A first fluidized bed pyrolysis reactor A1, a second fluidized bed pyrolysis reactor A2, an oxygen-depleted combustion tank 2, an oxygen-rich combustion tank 4, a cyclone separator 5, a solid feeding device 3, a first fractionation tower 6, a second fractionation tower 7, an oil-water separator at the top of the first fractionation tower 8, and an oil-water separator at the top of the second fractionation tower 9; a raw material mixing tank 10;

[0045] The solid slurry B feed pipeline S1, the carrier pipeline to be generated S2, the regenerated carrier pipeline S3, the first fluidized bed reactor A2 high-temperature oil and gas pipeline S4, the oxygen-lean combustion tank unloading coke pipeline S5, the oxygen-rich combustion tank returning the coke pipeline S15 to the oxygen-lean combustion tank, the oxygen-rich combustion tank returning the oxygen-lean combustion tank high-temperature flue gas pipeline S6, the oxygen-rich combustion tank unloading line S7, the oxygen-lean combustion tank high-temperature flue gas pipeline S10, the cyclone separation tank top high-temperature flue gas pipeline S12, the cyclone separation tank bottom discharge solid pipeline S11, the oxygen-lean combustion tank to the first fluidized bed reactor A1 regeneration coke line S9, the first fluidized bed reactor A1 to the oxygen-lean combustion tank to be generated coke line S8, the first fluidized bed reactor A1 high-temperature oil and gas pipeline S13;

[0046] Solid-containing slurry A feed pipeline S40, solid-containing slurry A mixed feed pipeline S14, solid-containing oil slurry pipeline S20 at the bottom of the first fractionation tower 6, circulating oil slurry pipeline S21 at the bottom of the first fractionation tower 6, external oil slurry pipeline S22 at the bottom of the first fractionation tower 6, external oil slurry pipeline S28 to the oxygen-depleted combustion tank at the bottom of the first fractionation tower 6, heavy oil production pipeline S23 of the first fractionation tower, medium oil production pipeline S24 of the first fractionation tower 6, light oil production pipeline S25 at the top of the first fractionation tower, sewage production pipeline S26 at the top of the first fractionation tower, and rich gas discharge S27 at the top of the first fractionation tower;

[0047] The solid-oil slurry pipeline S30 at the bottom of the second fractionation tower 7, the circulating oil slurry pipeline S31 at the bottom of the second fractionation tower 7, the external oil slurry pipeline S37 at the bottom of the second fractionation tower 7, the heavy oil production pipeline S33 of the second fractionation tower 7, the medium oil production pipeline S34 of the second fractionation tower 7, the light oil production pipeline S35 at the top of the second fractionation tower 7, the sewage production pipeline S36 at the top of the second fractionation tower 7, and the rich gas discharged from the top of the second fractionation tower 7 S37;

[0048] Preheat air S50 and S51, stripping steam S52 and S53. DETAILED DESCRIPTION

[0049] Exemplary embodiments of the present invention are described below, including various details of embodiments of the present invention to facilitate understanding, which should be considered as merely exemplary. Therefore, it should be appreciated by those of ordinary skill in the art that various changes and modifications may be made to the embodiments described herein without departing from the scope and spirit of the present invention. Similarly, for clarity and simplicity, the description of known functions and structures is omitted in the following description. Reagents, materials and devices used in the following embodiments, if not otherwise specified, can all be purchased commercially.

[0050] Example 1

[0051] Raw material A coal tar is transported to the first fluidized pyrolysis reactor A1 by a 1000kg / hr pipeline. The ash solid content of raw material A coal tar is 12%, mainly metal oxides. After being mixed with the high-temperature solid slurry at the bottom of the tower in the raw material mixing tank 10, it is atomized by the nozzle feeding system to small droplets of 100-300μm and enters the fluidized pyrolysis reactor A, where pyrolysis reaction occurs, generating high-temperature oil and gas and a large amount of coke. Under the reaction conditions of the first fluidized pyrolysis reactor A1 with a temperature of 580°C, a pressure of 0.1-0.25MPa, and an empty tower gas velocity of 0.55-1.0m / s, thermal cracking and condensation reactions occur to obtain reaction oil and gas, coke and solid inorganic matter, and the coke yield of coal tar is 11.11%. 800kg / hr of indirect liquefied slag wax of raw material B enters the second fluidized pyrolysis reactor A2 through the solid feeding device solid 3. The solid content of the indirect liquefied slag wax is 56%, mainly filter aids and iron catalysts. Thermal cracking and a very small amount of condensation reaction occur under the conditions of 560°C, 0.1-0.25MPag, and 0.55-0.8m / s of empty tower gas velocity in the second fluidized pyrolysis reactor A2 to obtain reaction oil and gas, coke and solid inorganic matter. The high-temperature oil and gas discharged from the top of the two reactors enter the oil and gas fractionation towers connected to each other to generate oil and gas products with different properties, which go to the downstream processing device.

[0052] The bottom oil slurry of the first fractionating tower 6 has a low solid content. After being mixed with the raw material A coal tar in a mixing tank at a ratio of 3%, the temperature of the raw material is increased. The bottom oil slurry and the raw material A coal tar enter the first fluidized bed reactor A1 through the nozzle atomization system to achieve the circulation treatment of the bottom slurry. In the first fluidized bed reactor A1, due to the high coking rate of the raw material, the fine powder particles can be used as the coking center, and the coking layers on the surface of the particles gradually grow, and the generated coke particles enter the oxygen-deficient coking tank.

[0053] The total heat required by the first fluidized pyrolysis reactor A1 is provided by the oxygen-depleted combustion tank 2 at a combustion temperature of 950°C through a coke particle circulation of 5000-8000 kg / hr. The heat required by the second fluidized pyrolysis reactor A2 is provided by the oxygen-rich combustion tank 4 at a combustion temperature of 950°C through a carrier circulation of 5000-6000 kg / hr. The coke production rate of the indirect liquefied slag wax is 1.81%. The excess coke particles discharged from the oxygen-depleted combustion tank 2 enter the oxygen-rich combustion tank 4 for further combustion. After the organic matter on the surface is burned clean, they are discharged from the system together with the solids in the raw material B of the second fluidized pyrolysis reactor A2 through the solid discharge line 7. The high-temperature flue gas at the top of the oxygen-rich combustion tank enters the oxygen-depleted combustion tank to supplement the heat for the oxygen-depleted combustion tank. The coke particle pipeline S15 from the oxygen-rich combustion tank to the oxygen-depleted combustion tank is only used when fluidization is started. Table 1 Main reaction results of coupled pyrolysis of coal tar and indirect liquefied slag wax - first fluidized pyrolysis reactor A1

[0054] Raw material name Coal tar part <![CDATA[Reaction temperature ( o °C)]]> 580℃ Ash-free yield wt% Dry gas yield (%) 2.91 LPG yield (%) 3.12 <180℃ Oil yield (%) 9.56 180-360℃ Oil yield (%) 46.51 360-520℃ Oil yield (%) 25.49 >520℃ oil yield (%) 1.11 Coke yield (%) 11.11 sum 99.81

[0055] Table 2 Main reaction results of coupled pyrolysis of coal tar and indirect liquefaction slag wax - second fluidized pyrolysis reactor A2

[0056]

[0057]

[0058] Note: The above data are all actual experimental data, so there are slight measurement errors and the sum is not 100%.

[0059] The above is only a preferred embodiment of the present invention. It should be pointed out that ordinary technicians in this technical field can make several improvements and supplements without departing from the method of the present invention. These improvements and supplements should also be regarded as the scope of protection of the present invention.

Claims

1. A fluidized bed coupling treatment method for solid-containing slurry, the method comprising: After raw material A is mixed with the high-temperature solid-containing slurry at the bottom of the first distillation tower (6) in the raw material mixing tank (10), it is atomized by the nozzle feeding system and enters the first fluidized pyrolysis reactor (A1), where a pyrolysis reaction occurs to generate high-temperature oil gas and coke. The high-temperature oil gas is discharged from the top of the reactor and enters the first distillation tower (6) to generate a tower top product and a high-temperature solid-containing slurry at the bottom of the tower. The coke is transported to the oxygen-depleted combustion tank (2); raw material B enters the second fluidized pyrolysis reactor (A2) through the solid feeding device (3), where a pyrolysis reaction occurs to generate high-temperature oil gas and coke. The oil and gas are discharged from the top of the reactor and enter the second distillation tower (7) to generate a tower top product and a tower bottom oil slurry; the tower top products of the two oil and gas distillation towers are respectively sent to downstream processing devices; wherein, both raw materials A and B are solid slurries, the solid content of raw material A is less than that of raw material B, and the coking rate of raw material A is higher than that of raw material B; the heat required by the first fluidized pyrolysis reactor (A1) is provided by the oxygen-poor combustion tank (2) through the circulation of coke particles; the heat required by the second fluidized pyrolysis reactor (A2) is provided by the oxygen-rich combustion tank (4) through the circulation of solid heat carriers.

2. The processing method according to claim 1, characterized in that: The heat required by the first fluidized pyrolysis reactor (A1) is provided by the oxygen-depleted combustion tank (2) through the circulation of coke particles. The high-temperature coke particles from the oxygen-depleted combustion tank (2) contact with the raw materials in the fluidized pyrolysis reactor (A1) to provide the required reaction heat and further undergo a pyrolysis reaction. The particle size increases and is discharged from the bottom of the reactor and enters the oxygen-depleted combustion tank (2). In the oxygen-depleted burner (2), the coke undergoes an oxidation reaction with oxygen, the particle size decreases, a portion of it is circulated back to the first fluidized pyrolysis reactor (A1), and the remaining portion enters the oxygen-rich combustion tank (4) to undergo a complete coke combustion reaction. After the reaction, only inorganic ash particles remain.

3. The processing method according to claim 1, characterized in that: The heat required by the second fluidized pyrolysis reactor (A2) is provided by the oxygen-enriched combustion tank (4) through the circulation of solid heat carrier. After the high-temperature heat carrier from the oxygen-enriched combustion tank (4) enters the second fluidized pyrolysis reactor (A2), it contacts with the raw material to cause a thermal cracking reaction of the raw material. A small amount of coke generated is attached to the heat carrier and returns to the oxygen-enriched combustion tank (4). In the oxygen-enriched combustion tank (4), the heat carrier with a small amount of coke attached and the coke from the oxygen-depleted combustion tank (2) contact with oxygen to cause a combustion reaction, thereby generating a large amount of heat. The coke is completely converted into gas including CO2. The temperature of the heat carrier increases, and a part of it is circulated back to the second fluidized pyrolysis reactor (A2). The excess heat carrier is discharged from the oxygen-enriched combustion tank (4) and discharged from the system after the heat is recovered.

4. The processing method according to claim 1, characterized in that: The high-temperature flue gas at the top of the oxygen-rich combustion tank (4) enters the oxygen-poor combustion tank (2) to replenish heat for the oxygen-poor combustion tank (2), and then returns from the oxygen-poor combustion tank (2) to the middle of the first fluidized pyrolysis reactor (A1), and then returns from the oxygen-rich combustion tank (4) to the middle of the second fluidized pyrolysis reactor (A2).

5. The processing method according to claim 3, characterized in that: The solid heat carrier can be a carrier such as quartz sand when starting up, and is gradually replaced by the solid inorganic matter generated in the second fluidized pyrolysis reactor (A2) as the reaction proceeds.

6. The processing method according to claim 1, characterized in that: The solid content of raw material A is 1-25%, and the coke yield is 2-30%; the solid content of raw material B is 5-55wt%, and the coke yield is 0.1-5wt%.

7. The processing method according to claim 1, characterized in that: The first fluidized pyrolysis reactor (A1) undergoes thermal cracking and condensation reaction at a temperature of 500-600°C, a pressure of 0.1-0.25 MPa, and an empty gas velocity of 0.55-1.0 m / s to obtain high-temperature oil and gas, coke, and solid inorganic matter; the second fluidized pyrolysis reactor (A2) undergoes thermal cracking and a very small amount of condensation reaction at a temperature of 500-580°C, a pressure of 0.1-0.25 MPa, and an empty gas velocity of 0.45-0.8 m / s to obtain high-temperature oil and gas, coke, and solid inorganic matter.

8. The processing method according to claim 1, characterized in that: The heat required by the first fluidized pyrolysis reactor is provided by the oxygen-poor combustion tank (2) through the coke circulation of 2000-8000 kg / hr, and the heat required by the second fluidized pyrolysis reactor is provided by the oxygen-rich combustion tank (4) through the carrier circulation of 2000-6000 kg / hr.

9. A fluidized bed coupled treatment device for solid slurry, the device comprising: A first fluidized pyrolysis reactor (A1), a second fluidized pyrolysis reactor (A2), an oxygen-depleted combustion tank (2), an oxygen-enriched combustion tank (4), a first fractionation tower (6), a second fractionation tower (7), a solid feeding device (3), and a raw material mixing tank (10).

10. The processing device according to claim 9, characterized in that In one embodiment, the top outlet of the first fluidized pyrolysis reactor (A1) is connected to the raw material inlet of the first fractionation tower (6), and the top outlet of the second fluidized pyrolysis reactor (A2) is connected to the raw material inlet of the second fractionation tower (7). The raw material mixing tank (10) is used to mix the raw material A and the high-temperature solid-containing slurry at the bottom of the first fractionation tower (6), and its outlet is connected to the raw material inlet of the first fluidized pyrolysis reactor (A1); the first fluidized pyrolysis reactor (A1) is used to pyrolyze the raw material A into high-temperature oil gas and coke, and the high-temperature oil gas enters the first fractionation tower (6), and the coke is transported to the oxygen-depleted combustion tank (2); the second fluidized pyrolysis reactor (A2) is used to pyrolyze the raw material B into high-temperature oil gas and coke, and the high-temperature oil gas enters the second fractionation tower (7).

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