CN103695057A - Method for preparing coal water slurry by using direct coal liquefaction residues, coal water slurry and gasification method thereof - Google Patents
Method for preparing coal water slurry by using direct coal liquefaction residues, coal water slurry and gasification method thereof Download PDFInfo
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
Abstract
The invention discloses a method for preparing coal water slurry by using direct coal liquefaction residues, the coal water slurry and a gasification method thereof. The method for preparing the coal water slurry by using direct coal liquefaction residues comprises the steps: S1, extracting the direct coal liquefaction residues, carrying out solid-liquid separation, and then, drying to obtain extracts; and S2, crushing and grinding the extracts, then, adding water and a selectable surfactant into the extracts, and stirring to obtain the coal water slurry. After the direct coal liquefaction residues are extracted, heavy oil and asphalt substances in the direct coal liquefaction residues can be separated from unconverted coal and ash which are both called as the extracts. After the extracts are crushed and ground and are filled with the water and the selectable surfactant, the coal water slurry can be formed. The coal water slurry can serve as a common fuel and can be particularly applied to gasification production. Therefore, the extracts of the direct coal liquefaction residues are effectively utilized, and furthermore, the utilization ratio and additional value of the direct coal liquefaction residues are increased.
Description
Technical Field
The invention relates to the field of recycling of direct coal liquefaction residues, in particular to a method for preparing coal water slurry by using direct coal liquefaction residues, the coal water slurry and a gasification method thereof.
Background
With the rapid development of national economy, the consumption of petroleum products in China is continuously increased, and the increase speed of the production quantity of crude oil in the same period is greatly exceeded. This results in the increasing of petroleum import quantity year by year, even exceeding the self-production quantity. China is a coal-rich and oil-poor country, advanced clean coal technologies such as fully utilizing rich coal resources and developing direct coal liquefaction are one of important ways of reducing excessive dependence on foreign crude oil, relieving the shortage of petroleum resources and the shortage of petroleum products in China, and are important measures for improving the utilization rate of coal resources in China, reducing coal pollution and promoting the coordinated development of energy, economy and environment.
The principle of direct coal liquefaction is to hydrogenate coal under high temperature and pressure and the action of a catalyst to directly convert the coal into clean transportation fuels (naphtha, diesel and the like) or chemical raw materials. The process of direct coal liquefaction generally comprises the steps of pre-grinding coal to a particle size of less than 0.15mm, mixing the coal with a solvent to prepare a coal slurry, and hydrogenating the coal slurry at a certain temperature (about 450 ℃) and under high pressure to crack and hydrogenate macromolecules in the coal into smaller molecules. Besides obtaining the required liquefied product in the direct coal liquefaction process, some hydrocarbon molecules and CO can be generatedXGas, process water and liquefaction residues (also called coal direct liquefaction residues) generated in the solid-liquid separation process. The direct coal liquefaction residue generally accounts for about 30% of the coal input. The utilization of the coal liquefaction residues has unappreciable influence on the efficiency of the liquefaction process, the economy and the environmental protection of the whole liquefaction plant, and the like. The research on the efficient and feasible comprehensive utilization method of the direct coal liquefaction residues can extract valuable products, and the method has important practical significance for improving the economic benefit of the direct coal liquefaction process.
The residue from direct coal liquefaction mainly consists of two parts, inorganic matter and organic matter, the organic matter includes liquefied heavy oil, asphalt and unconverted coal, and the inorganic matter (usually called ash) includes the mineral matter in coal and added catalyst. Wherein the liquefied heavy oil and asphalt substances in the organic substances account for about 50 percent of the total amount of residues, the unconverted coal accounts for about 30 percent of the total amount of the residues, and the ash accounts for about 20 percent of the total amount of the residues. Therefore, about 50% of asphalt substances and heavy oil in the direct coal liquefaction residue are separated for comprehensive development and utilization, and more valuable products can be extracted or prepared from the asphalt substances and the heavy oil; it is also necessary to exploit the unconverted coal and ash, which make up about 50% (collectively referred to as raffinate).
At present, the coal liquefaction residues are mainly combusted, coked to prepare oil, gasified to prepare hydrogen and other traditional methods. The direct combustion of the coal as fuel in a boiler or a kiln will undoubtedly affect the economy of coal liquefaction, and the higher sulfur content in the direct coal liquefaction residue will bring about environmental pollution problems. Although the yield of liquid oil in the coal liquefaction process is increased by coking oil preparation, the residue obtained by direct coal liquefaction cannot be utilized most reasonably, and the utilization ways of semicoke and coke are not very clear. The method for producing hydrogen by gasifying the coal direct liquefaction residues is an effective large-scale utilization way, but the high value-added utilization potential of asphalt substances and heavy oil in the residues is not reflected.
Solvent extraction is a method for effectively separating liquefied heavy oil and asphalt substances from unconverted coal and ash in coal liquefaction residues. Chinese patent CN101885976A discloses a method for extracting asphaltic substances and liquefied heavy oil from coal liquefaction residues, which adopts distillate oil produced in the direct coal liquefaction process as an extraction solvent to extract and separate asphaltic substances and liquefied heavy oil together. And separating the asphalt substances from the liquefied heavy oil by adopting a dry distillation method to obtain an asphalt intermediate phase. The liquefied heavy oil is returned to the coal liquefaction unit after being moderately hydrogenated. In the method, the liquefied heavy oil mainly consists of fractions with the temperature of more than 350 ℃, and the bonding force of the liquefied heavy oil and the asphalt substances is stronger. When the separation is carried out by adopting a high-temperature dry distillation method, the coking is caused, and the separation is difficult to be used as a circulating solvent for coal liquefaction. Chinese patents CN101962560A and CN101962561A disclose a method for extracting heavy liquefied oil and asphalt substances from coal liquefaction residues by using two-stage extraction, in which two different oil products produced in the direct coal liquefaction process are used as extraction solvents, and the two-stage sequential extraction is respectively performed on the liquefaction residues to obtain the heavy liquefied oil and the asphalt substances. The method can obtain the liquefied heavy oil and the asphalt substances, and develops and utilizes the liquefied heavy oil and the asphalt substances, but the method does not relate to the development and utilization of the raffinate of the direct coal liquefaction residue.
For the above reasons, it is necessary to design a method for utilizing raffinate of coal direct liquefaction residue to improve the utilization rate and added value of the coal direct liquefaction residue.
Disclosure of Invention
The invention aims to provide a method for preparing coal water slurry by using direct coal liquefaction residues, the coal water slurry and a gasification method thereof, so as to solve the problem of insufficient utilization of the direct coal liquefaction residues in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a method for preparing coal water slurry from coal direct liquefaction residues, comprising the steps of: s1, extracting the direct coal liquefaction residues, carrying out solid-liquid separation, and drying to obtain an extract residue; and S2, crushing and grinding the raffinate, adding water and an optional surfactant into the raffinate, and stirring to obtain the coal water slurry.
Further, in the step S2, the raffinate is mixed with coal, crushed and ground, and then water and an optional surfactant are added thereto, and the mixture is stirred to obtain the coal water slurry.
Further, in the step S2, the mass ratio of the raffinate to the coal is 1:0.1 to 1: 20.
Further, in the step S2, the particles with an average particle size of 0.05 to 1.0mm are obtained by crushing and grinding, preferably, the solid content in the coal water slurry is 50 to 80wt%, and the content of the surfactant is 0.1 to 1.0wt% of the total solid content in the coal water slurry.
Further, in the step S2, the coal is coking coal, low metamorphic bituminous coal or lignite; the surfactant is anionic, cationic or nonionic.
Further, the step S1 includes the following steps: s11, adding the direct coal liquefaction residues into an extraction solvent according to the mass ratio of 1: 1-1: 10, and introducing N into the extraction solvent2Or H2Pressurizing to 0.1-1.0 MPa, heating to 80-280 ℃, and stirring at a stirring speed of 50-300 r/min for 5-60 min to obtain a mixture; s12, carrying out solid-liquid separation on the mixture, and drying to obtain raffinate with the solid content of more than 95 wt%.
Further, in step S11, the extraction solvent is tetrahydrofuran, furfural, N-methylpyrrolidone, quinoline, direct coal liquefaction oil, distillate of direct coal liquefaction oil, coal tar, or coal tar distillate.
Further, in the step S12, the mixture is subjected to solid-liquid separation by a vacuum hot-filtration method, a hot-press filtration method, a gravity settling separation method, a cyclone separation method, a centrifugal separation method, or a distillation separation method; wherein, when the solid-liquid separation is carried out by adopting a vacuum hot suction filtration method, the pressure is 0.02KPa to 101.3KPa, the temperature is 50 ℃ to 250 ℃, and the preferable temperature is 150 ℃ to 200 ℃; when the hot-pressing filtration method is adopted for solid-liquid separation, the pressure is 0.2MPa to 1.0MPa, the temperature is 50 ℃ to 250 ℃, and the preferable temperature is 150 ℃ to 200 ℃; when the solid-liquid separation is carried out by adopting a cyclone separation method, the temperature is 50-250 ℃, and the inlet pressure is 0.2-0.6 MPa; when the centrifugal separation method is adopted for solid-liquid separation, the temperature is 50-180 ℃, and the inlet pressure is 0.1-0.6 MPa.
According to another aspect of the invention, a coal water slurry is provided, which is prepared by the method.
According to another aspect of the invention, a gasification method of the coal water slurry is also provided, wherein the gasification pressure of the coal water slurry is 3.0-4.5 MPa, and the gasification temperature is 1250-1550 ℃.
By applying the method for preparing the coal water slurry by using the direct coal liquefaction residue, the coal water slurry and the gasification method thereof, heavy oil and asphalt substances in the direct coal liquefaction residue can be separated from unconverted coal and ash (raffinate) after the direct coal liquefaction residue is extracted. The coal water slurry can be formed after crushing and grinding the raffinate and adding water and optional surfactant. The coal water slurry can be used as common fuel and can be used in gasification production. In conclusion, the method effectively utilizes the raffinate of the coal direct liquefaction residue, and further improves the utilization rate of the coal direct liquefaction residue.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail with reference to examples.
As described in the background section, the utilization rate of the generated coal direct liquefaction residue is low in the process of coal direct liquefaction. In order to solve the problem, the inventor of the invention provides a method for preparing coal water slurry by directly liquefying coal residues, which comprises the following steps: s1, extracting the direct coal liquefaction residues, carrying out solid-liquid separation, and drying to obtain an extract residue; and S2, crushing and grinding the raffinate, adding water and an optional surfactant into the raffinate, and stirring to obtain the coal water slurry.
In the method for preparing the coal water slurry by using the direct coal liquefaction residues, after the direct coal liquefaction residues are extracted, heavy oil and asphalt substances in the direct coal liquefaction residues can be separated from unconverted coal and ash, and the unconverted coal and the ash are collectively called as raffinate. The coal water slurry can be formed after crushing and grinding the raffinate and adding water and optional surfactant. The coal water slurry can be used as common fuel and can be used in gasification production. In summary, the method provides a recycling method for raffinate obtained by extracting the coal direct liquefaction residue, thereby improving the utilization rate of the coal direct liquefaction residue.
In the above method, the available coal-water slurry can be obtained by adding water and optional surfactant to the raffinate. In a preferred embodiment, in step S2, the raffinate is mixed with coal, crushed and ground, and then water and optionally a surfactant are added thereto, followed by stirring, to obtain the coal-water slurry. After the raffinate is mixed with coal, ash in the raffinate can be diluted. Thereby reducing the deashing burden in the later gasification production and improving the effective carbon content in the coal water slurry. In addition, the way of grinding the raffinate and the coal can adopt rod milling, ball milling or superfine stirring milling, as long as the particle sizes of the raffinate and the coal can be reduced.
In the above method, the raffinate and coal may be mixed in any proportion. In a preferred embodiment, in the step S2, the mass ratio of the raffinate to the coal is 1:0.1 to 1: 20. The coal water slurry obtained according to the proportion range can dilute ash in the residue raffinate, so that the deashing burden in the later gasification production can be reduced, and the effective carbon content in the coal water slurry can be increased. Meanwhile, the extraction residues and the coal are mixed according to the proportion, so that the stability of the coal water slurry is better on the basis of diluting ash in the coal water slurry.
It is within the ability of one skilled in the art, given the above teachings of the present invention, to select a particular configuration process for preparing the raffinate to form a coal-water slurry. In a preferred embodiment, the crushing and grinding in step S2 obtain particles with an average particle size of 0.05-1 mm. The coal water slurry of the raffinate with the particle size range has stronger suspension force of solid particles, so that the problem of poor fluidity caused by solid phase precipitation can be solved. Meanwhile, the coal water slurry has higher stability, the gasification effect of the coal water slurry can be promoted, and particularly, when the extraction residues and coal are mixed and simultaneously crushed and ground to obtain particles with the average particle size of 0.05-1 mm, the stability of solid and liquid phases in the coal water slurry can be improved.
In the method, the coal water slurry protected by the invention can be obtained by forming the raffinate or the mixture of the raffinate and the coal into slurry, and in a preferred embodiment of the invention, the solid content of the coal water slurry is 50-80 wt%, and the content of the surfactant is 0.1-1.0 wt% of the total solid content in the coal water slurry. The solid content in the coal water slurry is controlled within the range, so that the coal water slurry has better fluidity under the condition of lower water consumption. In addition, the surfactant is not an essential raw material in the coal water slurry, but the surfactant is controlled within the range, so that the compatibility of solid particles in the coal water slurry and a water phase can be improved, and the stability of the coal water slurry is further improved.
In the method, the coal which can be used comprises, but is not limited to, coking coal, low-rank bituminous coal or lignite, the ash content of the coal is low, the coal water slurry formed after the coal water slurry is mixed with raffinate is low, and the ash removal burden in the gasification process can be further reduced. In addition, surfactants that may be employed in the above-described methods include, but are not limited to, anionic, cationic, or nonionic surfactants. Wherein the anionic surfactant includes, but is not limited to, sodium dodecylbenzene sulfonate, sodium dodecyl sulfate, or triethanolamine soap; cationic surfactants include, but are not limited to, octadecyl trimethyl ammonium chloride, benzalkonium chloride, or benzalkonium bromide; nonionic surfactants include, but are not limited to, fatty acid glycerides, polysorbates, or sorbitan fatty acids. The surfactants can improve the compatibility between the coal powder, the solid particles of the residue raffinate and water, so that the coal water slurry has higher stability.
In the method, the residue after direct coal liquefaction is extracted to obtain the raffinate. In a preferred embodiment, the step S1 includes the following steps: s11, adding the direct coal liquefaction residues into an extraction solvent according to the mass ratio of 1: 1-1: 10, and introducing N into the extraction solvent2Or H2Pressurizing to 0.1-1.0 MPa, heating to 80-280 ℃, and stirring at a stirring speed of 50-300 r/min for 5-60 min to obtain a mixture; s12, carrying out solid-liquid separation on the mixture, and drying to obtain raffinate with the solid content of more than 95 wt%. Introducing N into the extraction system2Or H2The extraction system can be in a protective atmosphere to avoid the oxidation of carbon-containing components in the system under later high-temperature conditions. In addition, the direct coal liquefaction residue is extracted according to the process method, which is beneficial to extracting the residueThe heavy oil, asphaltenic matter of (a) are more effectively separated from unconverted coal and ash. Thereby further improving the utilization rate of the direct coal liquefaction residue.
The extraction solvent used in the above method is only required to be one in which the heavy oil and the asphaltic substances in the residue are easily soluble and the unconverted coal and the ash are hardly soluble. Preferably, the extraction solvent includes, but is not limited to, tetrahydrofuran, furfural, N-methylpyrrolidone, quinoline, coal direct liquefaction oil, distillate of coal direct liquefaction oil, coal tar or coal tar. Wherein, the direct coal liquefaction oil refers to a liquefaction product obtained by hydrogenating coal at high temperature and high pressure, and the distillate oil of the direct coal liquefaction oil refers to fractions with different distillation ranges (such as coal liquefaction light oil, coal liquefaction middle oil and coal liquefaction heavy oil) obtained by distilling the direct coal liquefaction oil; similarly, the distillate of coal tar refers to the distillate of different distillation ranges (such as coal tar light oil, phenol oil, wash oil, naphthalene oil and anthracene oil) produced by distilling coal tar under different temperature conditions. The extraction solution using the solvent as the residue can separate heavy oil and pitch substances from unconverted coal and ash in the residue more effectively. Thereby further improving the utilization rate of the direct coal liquefaction residue.
In the above method, the mixture may be subjected to solid-liquid separation by any method including, but not limited to, vacuum hot filtration, hot pressure filtration, gravity settling separation, cyclone separation, centrifugal separation or distillation separation. It is within the ability of one skilled in the art, among others, to select specific process conditions for each process. Preferably, when the solid-liquid separation is carried out by adopting a vacuum hot suction filtration method, the pressure is 0.02KPa to 101.3KPa, the temperature is 50 ℃ to 250 ℃, and the preferable temperature is 150 ℃ to 200 ℃; when the hot-pressing filtration method is adopted for solid-liquid separation, the pressure is 0.2MPa to 1.0MPa, the temperature is 50 ℃ to 250 ℃, and the preferable temperature is 150 ℃ to 200 ℃; when the solid-liquid separation is carried out by adopting a cyclone separation method, the temperature is 50-250 ℃, and the inlet pressure is 0.2-0.6 MPa; when the centrifugal separation method is adopted for solid-liquid separation, the temperature is 50-180 ℃, and the inlet pressure is 0.1-0.6 MPa. The solid-liquid separation methods are favorable for fully separating the solid phase from the liquid phase in the mixture, and particularly, the process conditions are controlled within the range, so that the solid-liquid separation effect is favorable.
In addition, the inventor also provides the coal water slurry which is prepared by the method. The coal water slurry formed by the method contains raffinate in the direct coal liquefaction residue, so that the direct coal liquefaction residue is completely and cleanly utilized.
In addition, the inventor of the invention further provides a gasification method of the coal water slurry, wherein the gasification pressure of the coal water slurry is 3.0-4.5 MPa, and the gasification temperature is 1250-1550 ℃. In addition, gasification units that may be employed include, but are not limited to, entrained flow beds and gasifiers. Under the condition, the coal water slurry is favorable for gasification reaction, so that the residue extraction residue of direct coal liquefaction in the coal water slurry is more effectively utilized.
The present invention is described in further detail below with reference to specific examples, which are not to be construed as limiting the scope of the invention as claimed.
Example 1
200kg of coal direct liquefaction residue and 2100kg of anthracene oil (distillation range of 220-405 ℃) are added into a stirring kettle, stirred at the speed of 45r/min, and filled with H2Heating to 1.5MPa, heating to 60 deg.C, stirring at constant temperature, and extracting for 70 min. The extraction mixture was subjected to hot vacuum filtration at a filtration temperature of 45 ℃ under a filtration pressure of 0.015kPa, the filter element pore size of the filter being 30 μm. After filtration, 141.3kg of solid residue and 2158.1kg of filtrate were collected.
The filtrate was sent to a vacuum distillation column for vacuum distillation, the extraction solvent was recovered at the top and side of the column for recycling, and 103.7kg of an extract (heavy oil, asphaltic substances) having an ash content of 0.2wt% was collected at the bottom of the column.
The solid residue was sent to a drying unit for drying, yielding 45.2kg of extraction solvent (recyclable) and 95.7kg of raffinate.
Mixing the raffinate and the lignite according to the ratio of 1:25 to obtain blended coal, crushing the blended coal, and performing ball milling to obtain particles with the average particle size of 1.5 mm. After adding water and an anionic additive (sodium dodecylbenzenesulfonate), an aqueous coal slurry was prepared in which the solid concentration was 45wt% and the additive content was 0.05wt% of the solid.
Feeding the coal water slurry into a gasification furnace for gasification, wherein the gasification pressure is 4.8MPa, the gasification temperature is 1610 ℃, and synthesis gas (CO + H) is obtained2）4147m3。
Example 2
200kg of coal direct liquefaction residues and 200kg of washing oil (distillation range is 220-405 ℃) are added into a stirring kettle, the stirring is carried out at the speed of 300r/min, and N is filled into the stirring kettle2Heating to 1.0MPa, heating to 280 deg.C, stirring at constant temperature, and extracting for 60 min. The extraction mixture was filtered under vacuum at 250 ℃ under 1.0MPa with a filter element having a pore size of 50 μm. After filtration, 135.1kg of solid residue and 263.8kg of filtrate were collected.
The filtrate was sent to a vacuum distillation column for vacuum distillation, the extraction solvent was recovered at the top and side of the column for recycling, and 99.8kg of extract (heavy oil, asphaltic substances) having an ash content of 0.5wt% was collected at the bottom of the column.
The solid residue was sent to a drying unit for drying, yielding 32.1kg of extraction solvent (recyclable) and 102.9kg of raffinate.
Mixing the raffinate and the lignite according to the ratio of 1:20 to obtain blended coal, crushing the blended coal, and performing ball milling to obtain particles with the average particle size of 0.05 mm. After adding water and an anionic additive (sodium lauryl sulfate) thereto, an aqueous coal slurry was prepared in which the solid concentration was 50wt% and the additive content was 1.0wt% of the solid.
Feeding the water coal slurry into a gasification furnace for gasification, wherein the gasification pressure is 3.0MPa, the gasification temperature is 1250 ℃, and synthesis gas (CO + H) is obtained2）2774m3。
Example 3
200kg of coal direct liquefaction residue and 2000kg of anthracene oil (distillation range of 220-405 ℃) are added into a stirring kettle, stirred at the speed of 50r/min, and N is filled into the stirring kettle2Heating to 0.1MPa, heating to 80 deg.C, stirring at constant temperature, and extracting for 5 min. The extraction mixture was filtered under vacuum at 50 ℃ under 0.2MPa with a filter element having a pore size of 10 μm. After filtration, 139.5kg of solid residue and 2058.7kg of filtrate were collected.
The filtrate was sent to a vacuum distillation column for vacuum distillation, the extraction solvent was recovered at the top and side of the column for recycling, and 104.7kg of an extract (heavy oil, asphaltic substances) having an ash content of 0.1wt% was collected at the bottom of the column.
The solid residue was sent to a drying unit for drying, yielding 44.3kg of extraction solvent (recyclable) and 93.9kg of raffinate.
Mixing the raffinate and the lignite according to the ratio of 1:0.1 to obtain blended coal, crushing the blended coal, and performing ball milling to obtain particles with the average particle size of 1 mm. After adding water and an anionic additive (sodium dodecyl benzene sulfonate) thereto, an aqueous coal slurry was prepared, wherein the solid concentration was 80wt% and the additive content was 0.1wt% of the solid.
Feeding the coal water slurry into a gasification furnace for gasification, wherein the gasification pressure is 4.5MPa, the gasification temperature is 1550 ℃, and synthesis gas (CO + H) is obtained2）120m3。
Example 4
300kg of coal direct liquefaction residue and 750kg of naphthalene oil (the distillation range is 120-210 ℃) are added into a stirring kettle, stirred at the speed of 60r/min, and N is filled into the stirring kettle2Heating to 0.2MPa, heating to 150 deg.C, stirring at constant temperature, and extracting for 30 min. Hot-pressing and filtering the extraction mixture, wherein the filtering temperature is 150 ℃, the filtering pressure is 0.3MPa, and the aperture size of a filter element of the filter is 30 mu m. After filtration, 180.1kg of solid residue and 867.3kg of filtrate were collected.
The filtrate was sent to a vacuum distillation column to be vacuum distilled, the extraction solvent was recovered at the top and side of the column to be recycled, and 145.9kg of an extract (heavy oil, asphaltic substances) having an ash content of 0.35wt% was collected at the bottom of the column.
The solid residue was sent to a drying unit for drying, yielding 31.7kg of extraction solvent (recyclable) and 146.6kg of raffinate.
Mixing the extraction residues and bituminous coal clean coal according to the proportion of 1:5 to obtain blended coal, crushing the blended coal, and performing ball milling to obtain particles with the average particle size of 0.1 mm. After water and a cationic additive (octadecyl trimethyl ammonium chloride) are added into the coal slurry, the coal slurry is prepared, wherein the solid concentration is 72.5wt%, and the additive content is 0.4wt% of the solid.
Feeding the coal water slurry into a gasification furnace for gasification, wherein the gasification pressure is 3.5MPa, the gasification temperature is 1400 ℃, and synthesis gas (CO + H) is obtained2）1466m3。
Example 5
250kg of coal direct liquefaction residue and 750kg of liquefaction medium oil (the distillation range is 150-310 ℃) are added into a stirring kettle, the stirring is carried out at the speed of 75r/min, and N is filled into the stirring kettle2Heating to 0.3MPa, heating to 170 deg.C, stirring at constant temperature, and extracting for 45 min. Hot-pressing and filtering the extraction mixture, wherein the filtering temperature is 120 ℃, the filtering pressure is 0.4MPa, and the aperture size of a filter element of the filter is 80 mu m. After filtration, 155kg of solid residue and 842.8kg of filtrate were collected.
The filtrate was sent to a vacuum distillation column for vacuum distillation, the extraction solvent was recovered at the top and side of the column for recycling, and 123kg of an extract (heavy oil, asphaltic substances) having an ash content of 1.6wt% was collected at the bottom of the column.
The solid residue was sent to a drying unit for drying, yielding 21.7kg of extraction solvent (recyclable) and 130.3kg of raffinate.
Mixing the raffinate and the low-rank bituminous coal into blended coal according to the ratio of 1:18, crushing the blended coal, and carrying out rod milling to form particles with the average particle size of 0.25 mm. After adding water and an anionic additive (octadecyl trimethyl ammonium chloride) thereto, an aqueous coal slurry was prepared in which the solid concentration was 50.1wt% and the additive content was 0.5wt% of the solid.
Feeding the water coal slurry into a gasification furnace for gasification, wherein the gasification pressure is 3.95MPa, the gasification temperature is 1350 ℃, and synthetic gas (CO + H) is obtained2）4100m3。
Example 6
200kg of coal direct liquefaction residue and 800kg of anthracene oil (distillation range is 220-405 ℃) are added into a stirring kettle, stirred at the speed of 85r/min, and N is filled into the stirring kettle2Heating to 0.15MPa, heating to 200 deg.C, stirring at constant temperature, and extracting for 27 min. The extraction mixture was filtered under hot vacuum at 180 ℃ under 2.9kPa, the filter element pore size of the filter being 30 μm. After filtration, 145kg of solid residue and 849kg of filtrate were collected.
The filtrate was sent to a vacuum distillation column for vacuum distillation, the extraction solvent was recovered at the top and side of the column for recycling, and 115kg of an extract (heavy oil, asphaltic substances) having an ash content of 0.4wt% was collected at the bottom of the column.
The solid residue was sent to a drying unit for drying, yielding 29.7kg of extraction solvent (recyclable) and 104.3kg of raffinate.
Mixing the raffinate and the lignite according to the ratio of 1:15 to obtain blended coal, crushing the blended coal, and performing ball milling to obtain particles with the average particle size of 0.15 mm. After adding water and an anionic additive (benzalkonium bromide), a coal water slurry was prepared, wherein the solid concentration was 65.6wt% and the additive content was 0.9wt% of the solid.
Feeding the coal water slurry into a gasification furnace for gasification, wherein the gasification pressure is 4.15MPa, the gasification temperature is 1270 ℃, and synthesis gas (CO + H) is obtained2）2781m3。
Example 7
Mixing 350kg of coalAdding the directly liquefied residue and 1000kg of coal tar distillate oil (distillation range is 200-260 ℃) into a stirring kettle, stirring at the speed of 55r/min, and filling N into the mixture2Heating to 0.15MPa, heating to 180 deg.C, stirring at constant temperature, and extracting for 50 min. And carrying out cyclone separation on the extraction mixture, wherein the separation temperature is 180 ℃, and the inlet pressure is 0.35 MPa. After the cyclone separation, 303kg of underflow concentrated solution and 1039kg of overflow clear solution are collected.
Sending the supernatant to a vacuum distillation tower, recovering the extraction solvent at the top and the side of the tower for recycling, and collecting 179kg of extract (heavy oil, asphaltic substances) with ash content of 4.9wt% at the bottom of the tower.
The underflow concentrate was fed to a drying unit for drying, yielding 119.7kg of extraction solvent (recyclable) and 176.3kg of raffinate.
Crushing the raffinate, and performing ball milling to form particles with the average particle size of 0.06 mm. After water and a nonionic additive (fatty acid glyceride) were added thereto, an aqueous coal slurry was prepared in which the solid concentration was 79.7wt% and the additive content was 0.1wt% of the solid.
Feeding the coal water slurry into a gasification furnace for gasification, wherein the gasification pressure is 3.15MPa, the gasification temperature is 1250 ℃, and synthesis gas (CO + H) is obtained2）125m3。
The measurement mode is as follows:
the coal water slurry prepared in the above embodiments 1 to 7 is subjected to characterization test, and the test method is as follows:
1) stability: and standing the prepared coal water slurry for 8 hours, and observing the solid settlement condition in the coal water slurry.
2) Rheological property: the apparent viscosity of the slurry is measured by an NXC-4C type coal-water slurry viscometer, and the rheological property of the slurry is inspected.
3) Fluidity: and (4) evaluating the fluidity of the coal water slurry by adopting a visual inspection method.
The results are shown in Table 1.
TABLE 1
From the above data and description, it can be seen that the coal water slurry prepared by the method of the above embodiment of the present invention using the raffinate of the coal direct liquefaction residue has a high apparent viscosity, indicating that it is not easy to settle. The coal water slurry has good fluidity, is continuously flowing or discontinuously flowing, and has good stability, and although some embodiments of the coal water slurry generate precipitates after standing for 8 hours, the precipitates can be suspended in the slurry again after stirring. The reason of the above aspects is that the coal water slurry prepared by the method in the embodiment of the invention can meet the transportation requirement of the coal water slurry.
Therefore, the method provided by the invention can fully utilize the raffinate in the direct coal liquefaction residue, and further increase the utilization rate and the additional value of the direct coal liquefaction residue.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for preparing coal water slurry by using direct coal liquefaction residues is characterized by comprising the following steps:
s1, extracting the direct coal liquefaction residues, carrying out solid-liquid separation, and drying to obtain an extract residue;
s2, crushing and grinding the raffinate, adding water and an optional surfactant into the crushed and ground raffinate, and stirring to obtain the coal water slurry.
2. The method according to claim 1, wherein in step S2, the raffinate is mixed with coal, crushed and ground, water and optionally a surfactant are added thereto, and the mixture is stirred to obtain the coal-water slurry.
3. The method according to claim 2, wherein in the step S2, the mass ratio of the raffinate to the coal is 1: 0.1-1: 20.
4. The method according to any one of claims 1 to 3, wherein the crushing and grinding in the step S2 are performed to obtain particles with an average particle size of 0.05-1.0 mm, and preferably, the content of the solid content in the coal water slurry is 50-80 wt%, and the content of the surfactant is 0.1-1.0 wt% of the total solid content in the coal water slurry.
5. The method according to any one of claims 1 to 4, wherein the coal in the step S2 is coking coal, low metamorphic bituminous coal or lignite; the surfactant is anionic, cationic or nonionic.
6. The method according to claim 1, wherein the step S1 comprises the steps of:
s11, adding the direct coal liquefaction residues into the extraction solvent according to the mass ratio of 1: 1-1: 10, and introducing N into the extraction solvent2Or H2Pressurizing to 0.1-1.0 MPa, heating to 80-280 ℃, and stirring at a stirring speed of 50-300 r/min for 5-60 min to obtain a mixture;
s12, carrying out solid-liquid separation on the mixture, and drying to obtain the raffinate with the solid content of more than 95 wt%.
7. The method according to claim 6, wherein in step S11, the extraction solvent is tetrahydrofuran, furfural, N-methylpyrrolidone, quinoline, coal direct liquefaction oil, distillate of coal direct liquefaction oil, coal tar, or distillate of coal tar.
8. The method according to claim 6, wherein in step S12, the mixture is subjected to solid-liquid separation by vacuum hot filtration, hot pressure filtration, gravity settling separation, cyclone separation, centrifugal separation or distillation separation; wherein,
when the vacuum hot suction filtration method is adopted for solid-liquid separation, the pressure is 0.02KPa to 101.3KPa, the temperature is 50 to 250 ℃, and the preferable temperature is 150 to 200 ℃;
when the hot-pressing filtration method is adopted for solid-liquid separation, the pressure is 0.2MPa to 1.0MPa, the temperature is 50 ℃ to 250 ℃, and the preferable temperature is 150 ℃ to 200 ℃;
when the cyclone separation method is adopted for solid-liquid separation, the temperature is 50-250 ℃, and the inlet pressure is 0.2-0.6 MPa;
when the centrifugal separation method is adopted for solid-liquid separation, the temperature is 50-180 ℃, and the inlet pressure is 0.1-0.6 MPa.
9. A coal water slurry prepared by the method of any one of claims 1 to 8.
10. The gasification method of a coal water slurry according to claim 9, wherein the gasification pressure of the coal water slurry is 3.0 to 4.5MPa, and the gasification temperature is 1250 to 1550 ℃.
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