슬러리 기포탑 반응기를 이용한 경유 및 휘발유 고함량 합성연료의 제조방법
The present invention refers to slurry bubble column by using the reactor of the synfuels via high gasoline and manufacturing method are disclosed. Coal liquefied (CTL) techniques using solid fuel coal fuel liquid such as gasoline and diesel oil convert high temperature and high pressure state and finally scheme conversion technology using a solvent, after the pin is indirect is dissolved in liquid fuel on a catalyst for converting coal gasification. Fischer - Tropsch synthesis reaction is 1923 years German chemist Fischer Tropsch (Fischer) (Tropsch) on a number of coal gasification by synfuels from synthesis gas tank is a technology for development the outdoors it stands first assault was on. Fischer - Tropsch synthesis reaction is a reaction wherein the conversion of synthesis gas using a catalyst, wherein the catalyst employed in the process selectivity timing is 5 or more carbon atoms general high catalyst productivity index of an hydrocarbon productivity and, carbon nanotubes can be overall efficiency. FT synthesis reaction is iron or cobalt catalyst and a reaction temperature of 10 - 30 200 provided 350 °C air pressure pressures of major reaction supporting body base 4 as follows. (A) chain growth reaction CO + 2H2 →- CH2- + H2 Δ H O (227 °C)=- 165kJ/mol (B) methanation CO + 3H2 CH→4 + H2 Δ H O (227 °C)=- 215kJ/mol (C) water gas shift reaction CO + H2 O ↔ CO2 + H2 Δ H (227 °C)=- 40kJ/mol (D) reaction [...] 2CO ↔ C + CO2 Δ H (227 °C)=- 134kJ/mol FT synthesis processes in the development of the reactor with catalyst based on advanced consisted primarily Sasol long development experience, initial fixed-bed reactor (Arge) to and in a circulating fluidized bed reactor (Synthol) on slurry reactor (Slurry) stationary fluidized bed reactor (Advanced Synthol) gradually to form advanced reactor FT priority order (also 1), recent Sasol slurry reactor in plant cost reduce existing multi-fixed-bed rotting use 25 - 30% compared report period to disclosed. Fixed-bed reactor and slurry reactor middle distillates (LTFT) process producing low temperature FT wax and a circulating fluidized bed reactor is mainly used stationary fluidized bed reactor producing mainly naphtha and olefins (HTFT) process and has high temperature FT known to table 1 efined each process product selectivity can be represented. The investment cost of the plant for reduction and enlargement process development FT reactor allowing development of techniques for the same large unit is decreased. However, this large supply of plant development of customized plant etc. is required taking into account the situation on-site difficult. In particular, a small-sized movable plant comprises location conditions than before the pin is simultaneously at a blade placement number one subject is gas. However, it is not developed CTL plant cladding techniques such small commercial level. The purpose of the invention using the slurry bubble column reactor cost efficiently formed on the height and the wax decreased production of methanol via the production of a number can be [...] method are disclosed. Fischer - Tropsch synthesis reaction using slurry bubble column reactor (SBCR) aspect of the present invention number 1 in synthesis gas catalyst containing the slurry so produced in a synthetic fuel number bath method, Slurry bubble column reactor containing catalyst slurry in step number 1; and Synthesis gas of the temperature 275 to 300 °C by adjusting said slurry bubble column reactor fed into a Fischer - Tropsch synthesis comprises the step of performing a number 2, Here, said catalyst is Fe: Cu: K: SiO2 =100:1 - 10:1 - 20:10 - 50 iron-based catalyst in weight, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith5-11 At least 29% by weight ratio of the hydrocarbon manufacturing method characterized a number [...] substrate. Aspects of the present invention number 2 coal or biomass yield using liquid hydrocarbons in a number bath method, Coal or biomass number a milling step; By supplying oxygen-containing gas to said ground coal or biomass gasification to yield for producing synthetic gas number b step; Slurry bubble column reactor containing catalyst slurry in step number 1; and Step coal synthesis gas fed into said number b of the temperature 275 to 300 °C to said slurry bubble column reactor is adjusted to a Fischer - Tropsch synthesis comprises the step of performing a number 2, Here, said catalyst is Fe: Cu: K: SiO2 =100:1 - 10:1 - 20:10 - 50 iron-based catalyst in weight, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith5-11 At least 29% by weight ratio of the hydrocarbon manufacturing method characterized a number [...] substrate. Hereinafter the present invention it relates to 2000. Generally hot FT reactor maintained at 300 °C and when, Synthol Advanced Synthol reactor (fluidized bed reactor) and using gasoline and light week lifestyle which contain these compounds, when a low temperature of 180 to 250 °C by operating low temperature FT reactor, fixed bed reactor on slurry bubble column reactor (SBCR) which uses the above-mentioned (Arge), the week lifestyle and wax process from production of gasoline and contain these compounds via by-products. In the present invention reaction slurry bubble column reactor (SBCR) existing FT application mainly low-temperature operation via the Fischer Tropsch synthesis reaction product increased unsaturated fatty acid content or gasoline production of wax than optimal process capable of producing [...] number can be found. In particular, fixed bed reactor SBCR reactor and fluidized bed reactor by applying a predetermined level of an industrial equipment cost and catalyst consumption 1/4, 1/4 level in reactor pressure drop as well as a primer may be least one catalyst in an ejection as well as lower cost with high efficiency via the center of gravity of the catalyst for producing or gasoline can be found. The present invention refers to the WIPO. As aforementioned, according to one aspect of the present invention Fischer - Tropsch synthesis reaction using slurry bubble column reactor (SBCR) synthesis gas so produced a number in a bath containing the slurry catalyst synfuels the method, Slurry bubble column reactor containing catalyst slurry in step number 1; and Synthesis gas of the temperature 275 to 300 °C by adjusting said slurry bubble column reactor fed into a Fischer - Tropsch synthesis comprises the step of performing a number 2, Here, said catalyst is Fe: Cu: K: SiO2 =100:1 - 10:1 - 20:10 - 50 iron-based catalyst in weight, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith5-11 29% by weight hydrocarbon ratio of greater than or disclosed. In the present invention, said steps including manufacturing method may be prepared by the number into a coal synthesis gas is disclosed. Coal or biomass number a milling step; and By supplying oxygen-containing gas to said ground coal or biomass gasification to yield for producing synthetic gas number b step. In addition as aforementioned, according to one aspect of the present invention yield using biomass coal or other liquid hydrocarbon bath method is a number, Coal or biomass number a milling step; By supplying oxygen-containing gas to said ground coal or biomass gasification to yield for producing synthetic gas number b step; Slurry bubble column reactor containing catalyst slurry in step number 1; and Step coal synthesis gas fed into said number b of the temperature 275 to 300 °C to said slurry bubble column reactor is adjusted to a Fischer - Tropsch synthesis comprises the step of performing a number 2, Here, said catalyst is Fe: Cu: K: SiO2 =100:1 - 10:1 - 20:10 - 50 iron-based catalyst in weight, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith5-11 29% by weight hydrocarbon ratio of greater than or disclosed. In the present invention, said number 1 and number 2 between catalyst activating step further includes a step number 1 - 1 can be reduced. Said number a step, coal or gasified biomass suitable for these state in comminuting are disclosed. Said number a step can be a wet or dry milling, wet in the case of water as the dispersion medium, C1-4 Alcohol or a combination of dispersion medium can be used. Specifically, in the case of wet coal crushed coarse fraction coal mill can be dispersed in water to form high pressure liquid coolant using coal slurry number. In addition, in the case of biomass, dry a grinding can be used in a powder form. The biomasses are cellulose (cellulose), hemicellulose (hemicellulose), lignin (lignin) natural polymer materials such as major component is exposed composites made huge itself can be referred to as a polymer material. In the present invention, woody biomass can be used as biomass. In said number a, coal or the biomasses are 75 micro m hereinafter, preferably designed as a 75 micro m to 200 micro m can be comminuted. Said number b step, said oxygen-containing gas as milled coal or biomass oxidation number of coal gasification to yield FT synthesis reaction for use as raw material for obtaining a synthesis gas are disclosed. In said number b, the pulverized coal or biomass and oxygen-containing gas in the gasifier and the gas burner in contact is equal to the reactor. In the present invention said number b step can be carried out in low pressure distribution. Specifically, said number b is 5 to 10 bar-temperature catalytic reaction of step can be conducted under pressure. In addition, a reaction temperature of 800 to 1300 °C said number b step gasification reaction can be conducted under. In slurry bubble column reactor containing catalyst slurry in said number 1 after applying, in said synthesis gas fed into said number 2 of the temperature 275 to 300 °C slurry bubble column reactor to Fischer - Tropsch synthesis reaction to produce hydrogen by adjusting hydrocarbon can. In the present invention said number 2 Fischer - Tropsch synthesis reaction in the performing, as a catalyst Fe: Cu: K: SiO2 =100:1 - 10:1 - 20:10 - 50 in weight and iron-based catalyst, the aforementioned 275 to 300 °C as slurry bubble column reactor fed into said Fischer - Tropsch synthesis reaction of the temperature by adjusting the number C extend the total product produced therewith5-11 29 weight % or more hydrocarbon product hydrocarbon ratio of the number [...] characterized. In the present invention, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith19+ 5 to 15% by weight of hydrocarbons ratio implementation being. In the present invention, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith5-11 C 29 to 35 weight % and the ratio of the hydrocarbon19+ 5 to 15% by weight of hydrocarbons ratio implementation being. In the present invention, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith5-11 C 29 to 35 weight % and the ratio of the hydrocarbon12-18 10 to 15% by weight of hydrocarbons and C ratio19+ 5 to 15% by weight of hydrocarbons ratio implementation being. In the present invention, Fischer - Tropsch synthesis reaction said number C extend the total product produced therewith1 C 10 to 17% by weight and the ratio of the hydrocarbon2-4 25 to 35% by weight of hydrocarbons and C ratio5-11 C 29 to 35 weight % and the ratio of the hydrocarbon12-18 10 to 15% by weight of hydrocarbons and C ratio19+ 5 to 15% by weight of hydrocarbons ratio implementation being. In the present invention, said synthesis gas is carbon monoxide and hydrogen or inert gas impurity carbon monoxide and hydrogen, methane, carbon dioxide mixed with either can be selected among people. In the present invention, said synthesis gas is carbon monoxide and hydrogen 1: are mixed at the ratio of 1 - 2, most preferably carbon monoxide and hydrogen produced from the well in as regards a product for obtaining rate ratio of 1:1, additionally comprising an inert gas is carbon dioxide or methane or other impurities can be. Said big volume ratio the ratio of carbon monoxide and hydrogen. The present invention the ratio of the Fischer - Tropsch reaction synthesis gas throughout so big in volume ratio. In the present invention, said synthesis gas space velocity is 2. 5 - 24. 0 NL/gCat In/hr can be supplied within the range. Said reaction progress too large even when less than than water is low productivity per unit time generating a number of hydrocarbons cannot be door mounted more synthesis gas when said space velocity conversions of carbon monoxide can be reduced. In the present invention reaction slurry bubble column reactor (SBCR) existing FT application mainly low-temperature operation via the Fischer Tropsch synthesis increased unsaturated fatty acid content or gasoline production of wax than optimum process capable of producing a reaction product can be [...] number. Figure 1 FT FT FT indicating the type of reactor used in hot and cold form are disclosed. In the embodiment of the present invention also Figure 2 shows a number of coarse general outline during jaws synfuels in one indicating system are disclosed. Hereinafter, the present invention through a corresponding business are provided in the embodiment as follows. In the embodiment of the present invention is generally described the present invention is to exemplify these for range and not the limited to those in the embodiment. In the embodiment 1: the present invention according to synfuels number bath As shown in fig. 2, FT reactor slurry bubble column reactor (SBCR) form FT reactor design is selected was to construct a system connected to the coal gasifying synfuels number numerical control machine. Specifically, when synthesizing FT reaction temperature such as a high pressure liquid coolant to table 2 to be set to 290 °C synfuels his number. Comparison example 1: existing hot FTFor fluidized bed reactor synfuels number tank and method of manufacturing In said in the embodiment 1, 2 also shown in number in a fluidized bed reactor for SBCR system numerical control machine synfuels instead to construct a system to replace the existing hot FT synfuels number numerical control machine was. Specifically, when synthesizing FT reaction temperature such as a high pressure liquid coolant to be set to 300 °C to table 3 synfuels his number. Experiment example 1: synfuels hydrocarbon compositions analysis Analyzing said in the embodiment 1 and comparison example 1 synthetic fuel hydrocarbon compositions of his number in high pressure liquid coolant. For table 4 shown to result. Through said table 2, according to the present invention SBCR 290 °C Fischer Tropsch synthesis reactor operating conditions existing mounted higher than under conditions when performing an electrochemical reaction, such as comparison example 1 hot FT synthesis reactor for hydrocarbon compositions for continuous high pressure liquid coolant fuel may be similar number has been confirmed. In particular, according to the present invention extend the complete product C synfuels prepared by the number5-11 Ratio of 29% by weight of at least C hydrocarbon12-18 10 to 15% by weight of hydrocarbons and C ratio19+ Hydrocarbon ratio of 20 weight % hereinafter can be generated not inserted, the overall synthetic fuel methanol production is increased and the wax production is reduced know via can be schedulable. The present invention relates to a method for producing synthetic fuel having high diesel and gasoline contents using a slurry bubble column reactor. The present invention can provide an optimal process which enables the production of a Fischer-Tropsch synthesis reaction product having increased diesel and gasoline contents, rather than the production of wax, by operating, at a high temperature, a conventional slurry bubble column reactor (SBCR) which has been mainly applied to a low-temperature FT reaction. Fischer - Tropsch synthesis reaction using slurry bubble column reactor (SBCR) in synthesis gas catalyst containing the slurry so produced, Fischer - Tropsch synthesis reaction C extend the total product prepared by the number5 - 11 At least 29% by weight ratio of hydrocarbons, C19 + 5 to 15% by weight ratio of the hydrocarbon fuel in a tank wherein number method, slurry bubble column reactor containing catalyst slurry in step number 1; and synthesis gas fed into said slurry bubble column reactor 300 °C to Fischer - Tropsch synthesis of the temperature 290 to adjusting comprises the step of performing a number 2, here, said catalyst is Fe: Cu: K: SiO2 =100:1 - 10:1 - 20:10 - 50 manufacturing method characterized in weight iron-based catalysts. Back number According to Claim 1, said Fischer - Tropsch synthesis reaction C extend the total product prepared by the number5-11 C 29 to 35 weight % and the ratio of the hydrocarbon19+ 5 to 15% by weight of hydrocarbons ratio in manufacturing method characterized. According to Claim 1, said Fischer - Tropsch synthesis reaction C extend the total product prepared by the number5-11 C 29 to 35 weight % and the ratio of the hydrocarbon12-18 10 to 15% by weight of hydrocarbons and C ratio19+ 5 to 15% by weight of hydrocarbons ratio in manufacturing method characterized. According to Claim 1, said Fischer - Tropsch synthesis reaction C extend the total product prepared by the number1 C 10 to 17% by weight and the ratio of the hydrocarbon2-4 25 to 35% by weight of hydrocarbons and C ratio5-11 C 29 to 35 weight % and the ratio of the hydrocarbon12-18 10 to 15% by weight of hydrocarbons and C ratio19+ 5 to 15% by weight of hydrocarbons ratio in manufacturing method characterized. According to Claim 1, number 2 and number 1 - 1 can activate the catalyst between said number 1 step further including reducing manufacturing method characterized. [Claim 7 (is) when the setting registration fee payment size abandoned.] According to Claim 1, said synthesis gas is carbon monoxide and hydrogen or inert gas impurity carbon monoxide and hydrogen, methane, carbon dioxide mixed with either selected among characterized using manufacturing method. According to Claim 1, said synthesis gas is carbon monoxide and hydrogen 1: manufacturing method characterized of using mixed at a rate of 1 - 2. According to Claim 1, said synthesis gas space velocity is 2. 5 - 24. 0 NL/gCat Characterized in supplied/hr within manufacturing method. [(Is) setting registration fee payment claim 10 when the blades abandoned.] According to Claim 1, including manufacturing method steps in said synthesis gas is a manufacturing method characterized prepared by the number: coal or biomass number a milling step; and said oxygen-containing gas supplying ground coal or biomass gasification to yield for producing synthetic gas number b step. Using coal or biomass as raw material, Fischer - Tropsch synthesis reaction C extend the total product prepared by the number5 - 11 At least 29% by weight ratio of hydrocarbons, C19 + 5 to 15% by weight of hydrocarbons in liquid hydrocarbons in a bath ratio number method, coal or biomass number a milling step; by supplying oxygen-containing gas to said ground coal or biomass gasification to yield for producing synthetic gas number b step; step number 1 contained catalyst slurry in slurry bubble column reactor; and said number b step 290 to 300 °C coal synthesis gas fed into said slurry bubble column reactor to Fischer - Tropsch synthesis of the temperature adjusting comprises the step of performing a number 2, here, said catalyst is Fe: Cu: K: SiO2 =100:1 - 10:1 - 20:10 - 50 manufacturing method characterized in weight iron-based catalysts. Product LTFT (180 provided 250 °C) HTFT (300 provided 350 °C) CH4 4 7 C2 To C4 Olefin 4 24 C2 To C4 Paraffin 4 6 Gasoline 18 36 Middle distillates 19 12 Heavy oil (heavy oil) and wax 48 9 Crab four [thu oxy 3 6 Temperature (°C) Pressure (Mpa) GHSV (NL/G (cat)- h) 290 1. 5 2. 80 Conversion (%) WGS Activity H2/CORatioinTail Gas Olefin/ParaffinRatioinC2-a C4 CO H2 H2 + CO. CO2 Sel. (%) Extent of WGS (Kp) 87. 68 63. 63 75. 51 44. 15 15. 50 3. 03 2. 58 Temperature (°C) Pressure (Mpa) GHSV (NL/G (cat)- h) 300 1. 75 2. 80 - 3. 50 Conversion (%) WGS Activity H2/CORatioinTail Gas Olefin/ParaffinRatioinC2-a C4 CO H2 H2 + CO. CO2 Sel. (%) Extent of WGS (Kp) 84. 20 54. 25 66. 70 54. 23 19. 57 3. 67 2. 88 CH4 (Wt %) C2-4 (Wt %) C5-11 (Wt %) C12-18 (Wt %) C19 + (wt %) Productivity (gHC/gcat provided h) In the embodiment 1 15. 2 32. 5 30. 1 10. 9 11. 3 0. 368 Comparison example 1 21. 2 33. 6 27. 68 10. 66 6. 82 0. 275
