• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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    • 专利摘要:
    A process for separating tar and solid particles from coal liquefaction products using a highly selective halogenated aliphatic solvent which removes essentially all the tar and solid particles from the coal liquefaction products wherein a minimum amount of energy is used. This is accomplished by contacting said coal liquefaction products with the halogenated aliphatic solvent to form two phases, one containing said tar and solid particles and the other containing said solvent and the remainder of said coal liquefaction products.
    公开号:SU904530A3
    申请号:SU782678408
    申请日:1978-10-20
    公开日:1982-02-07
    发明作者:Анджело Параскос Джон；Вилльям Смит Эдвард
    申请人:Галф Рисерч Энд Дивелопмент Компани (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to methods for separating tar and solid particles from coal dilution products, carried out in the presence of hydrogen and a solvent, and can be used in the coal chemical industry. The problem of removing or separating suspended solids and tar from a stream of liquefied coal occurs in all industries associated with the use of coal dilution products. In the production of synthetic carbon from liquid carbon, coal is usually crushed, mixed with a solvent to form a slurry, and enriched by tiding. At the same time, carbon dilution products with entrained solid particles, tar and the like are obtained. Traditional solutions to this problem include distillation, evaporation, filtration, settling and centrifugation to remove solid particles. Distillation or filtration is most commonly used. However, the cost of the cost of heat and energy in such methods can lead to its industrial inapplicability. In addition, solid particles in the boiling fraction, located high near the surface, strongly adsorb liquids. Therefore, the complete removal of liquid from solid particles, both from ash and from non-transformed coal, is difficult. In addition, a certain amount of liquid must be left in the solid phase in order to maintain the fluidity of the residual fraction in order to remove the latter from the vacuum evaporator or vacuum distillation device. The closest to the proposed invention is a method for separating tar and solid particles from coal liquefaction products by mixing the raw material with a solvent, which uses an oil fraction, in particular a kerosene fraction, 5 of which boils at 121 C 3-9 and 95 at $ 177 C. The characterizing factor of such a solvent is K -UTv / C; 9, 75. where Tg is the average molecular boiling point, G is the specific gravity at 15, and the weight ratio is liquid promoter: carbon-thinning products is 0.2: 1-3: 1. Gravitational sedimentation in the presence of such a solvent is carried out at 1–9–315 ° C, pressure of 0–35 atm. The solvent is then distilled off and returned to mixing with the feedstock. The degree of separation of solid particles is / 98.7% (their content in the target product is - / O, 03%). The purpose of the invention is to simplify the process technology. This goal is achieved by the method of separation of tar and solid particles of coal from coal dilution products containing solid particles with a diameter of 0.1-70 µm by mixing them with a solvent, which is trichlorotrifluoroethane, taken in a volume ratio of the dilution product: trichlorotrifluoroethane, equal to 0.5 1-5: 1 for 0.560 minutes to obtain an upper phase containing tar and solid particles and a lower phase containing solvent and other products of coal dilution, followed by separation of these phases, distilling off the solvent and returning it to the mix. The drawing shows a schematic diagram of a device that implements the proposed method. The crushed coal and oil (coal solvent) are fed along the line to the slurry zone 2, where they are mixed with the solvent coming along line 3 and, together with the hydrogen fed through line k, are supplied to the dilution zone 5 containing the hydrogenation catalyst . Hydrogen is supplied to line k from recirculation line 6, and, if necessary, according to line 7- Coal liquefaction product obtained in liquefaction zone 5 as a result of the usual hydrogenation process is directed along line 8 to zone 9 mixed with trichlorotrifluoromethane, which is fed to line 8 through lines 0-12., Trichlorofluoromethane and coal liquefaction product containing tar and / or solid particles are thoroughly mixed and then sent along line 13 to separation zone k or hydroclone 15, where the liquefaction product is , tar and solids are separated with the image vaniem lower phase comprising coal liquefaction product without tar and / or solids and trichlorofluoromethane, and an upper phase comprising tar and / or solid particles and some amount of entrained trichlorofluoromethane. The lower phase is fed through line 16 to the solvent purification zone 17, where the solvent is cleared of oil using heat exchanger 18, trichlorofluoromethane is withdrawn through line 19. The oil is directed along lines 20 and 21 to the collecting device, and some of the oil is returned to the slurry zone 2 through line 3- The upper phase, containing tar and / or solids and solvent, is fed through line 22 to the solvent purification zone 23, in which the solvent is cleaned of tar and / or solid products using a heat exchanger 2 and through lines 11 and 12 return to mixing zone 9. Tar and solid particles can be supplied via line 25 to gas production zone 26, into which steam is introduced through line 27. In the gas production zone 2b, the exothermic reaction of free oxygen with tar and solid particles occurs, in which carbon dioxide, carbon monoxide, water vapor, methane and heat are released. Hydrogen is produced by secondary reactions. The vapor shifts the reaction towards the evolution of hydrogen. The tar and W produced in the gas production zone 26 are directed through line 28 to a collecting device (not shown), hydrogen and other components are sent to line 29 to the hydrogen enrichment zone 30, from which carbon monoxide, carbon dioxide and methane are removed lines 31 to a collecting device (not shown). Hydrogen is fed through line 6 to line 7, then to line k and to zone 5 of the dilution coal. According to the proposed method, it is possible to recycle any product of coal liquefaction containing tar and solid particles. Coal liquefaction products, which are liquid synthetic fuels obtained from solid carbonaceous substances, should be obtained by mixing the crushed carbonaceous material, such as coal, with a solvent, resulting in a suspension. The suspension is introduced into a reaction vessel containing a conventional hydrogenation catalyst, for example, nickel, cobalt, molybdenum, titanium or tungsten or mixtures thereof on an aluminum base, and is reacted at ordinary temperatures and pressures of the hydrogenation process.
    An external source of hydrogen, used in conjunction with a hydrogenation catalyst, is introduced into the reaction vessel. Hydrogen can also be used without a catalyst, for example, in the topic of carbon solvent recovery. After hydrogenation, the resulting liquified coal products are separated by the proposed method. Received
    (Products are distilled to obtain fractions with different boiling points. Some of these products can be used as fuels. Others can be enriched using processes such as cracking, hydrocracking, etc.
    Synthetic liquid fuels derived from coal, in terms of aromatics, boil from 38 to., Have a density of from 0.9 to 1.1. The molecular ratio of carbon to hydrogen is 1.3: 1. to 0.66: 1.
    The composition of the coal used to obtain the liquefaction products is presented in Table. one.
    Table 1
    The presence of carbon and hydrogen in coal is mainly associated with benzene compounds, multiring aromatic compounds, heterocyclic compounds, etc. Nitrogen is present as chemically bound with aromatic compounds. A certain amount of sulfur and oxygen is in the form of chemically bound with aromatic compounds, and some with non-limiting elements, such as iron and calcium. Such coal includes, for example, anthracite, bituminous and sub-bituminous coals, brown coal and other types of coal. If raw COAL is used, the best results are obtained when the carbon content in dry coal does not exceed 86 wt.%, And dry volatiles are at least weight. in terms of desalted coal. Before liquefaction, the coal is ground in a grinding machine, for example, in a hammer mill, to such an extent that at least 50% by weight of the coal is sifted through a sieve with a mesh size of tO mesh. The crushed carbon is dissolved or suspended in a suitable solvent. V. tab. 2 is represented; the composition of the coal, the solvent - anthracene oil and the suspension of the oil and the suspension of oil and the suspension of coal in the oil used to obtain the products of coal liquefaction. It is possible to use Dittsburg coal, anthracene m
    It is possible to use Kentucky coal, anthracene oil, and Susc. Table 2
    Table 3
    penza, the composition of which is given in table. . oil and suspension, the composition of which is given in table. 3
    The weight ratio of solvent to the original coal may be 0.6: 1 - 9: 1 preferably Irl-irl 55 The best results are achieved when this ratio is 2: 1 It is possible to use a weight ratio that exceeds, but additional advantages when dissolving or suspending coal. This technique does not. It is not advisable to inject an excess amount of solvent, since additional energy consumption is required for the subsequent separation of the solvent. The solvent used to form a paste is any liquid compound, or a mixture of such compounds that can serve as a carrier of hydrogen. However, it is preferable to use liquid aromatic hydrocarbons. A more rational solvent is anthracene oil. It is also possible to use solvents such as polycyclic aromatic hydrocarbons, in particular naphthalene and chrysene, and their hydrogenation products, such as tatralin (tetrahydronaphthalene), decalin, etc., or one of these compounds in a mixture with a phenolic compound, for example phenol or cresol .. This solvent is used at the beginning of the process. Further, the solvent used is the liquid fraction obtained by hydrogenation, which is produced in an amount sufficient to replace any amount of solvent that has become other substances or is lost in the process. As the process proceeds, the solvent used at the beginning of the process is gradually diluted with the liquid fraction produced during the process. Thus, at the end of the process, the recycled stream is essentially free of the original solvent. If the method is carried out in semi-continuous mode, the solvent used at the beginning of each new period can be obtained in the previous operation. Such solvents derived from coal are aromatic with a boiling range from U9 to 7bO ° C, specific gravities from 0.9 to 1, 1j and an atomic ratio of carbon to hydrogen of up to 1.5: 1 to 0.56: one. The solvent obtained during the processing of sub-bituminous coal, such as Weisming-Montana coal, contains an average oil with a typical boiling range from 191 to 357 ° C. The hydrogenation process is carried out at a temperature of 2 ° C - atm, preferably atm. 105 280, atm, with an average weight rate of 1 hour per hour, ranging from 0.25 to 50 kg of solid carbonaceous material per 1 kg of catalyst per 1 h, Hydrogen is added in the amount of 35635 mM VM suspension. The specific selection of boron conditions depends, for example, on the catalyst, on the type of feedstock, on the degree of conversion required. It is advisable to use as low as possible acceptable temperature. This is due to the fact that high temperatures lead to undesirable effects, such as coking. In particular, if the hydrogenation catalysts are exposed to high temperatures, their service life is reduced. The hydrogen recycling rate varies little for different materials and in the preferred embodiment, is 3561/80 suspensions. Any known hydrogenation catalyst may be used. It is impractical to use a catalyst containing at least one hydrogenation component selected from the group consisting of metals, sulfur metals and / or oxides of metals of group U1 and VIII of the periodic table. In particular, nickel, cobalt, molybdenum and tungsten are used as hydrogenating metals. The most effective catalysts A contain from 2 to 25 wt.% (In the preferred embodiment, from i to 16 weight D) molybdenum and at least one of the metals of the iron group on a porous base, and the metals of the iron group are present in such quantities that their atomic ratio to molybdenum does not exceed 1.0. Catalysts B contain from 5 to kO weight. | (in the preferred embodiment, from 10 to 25 weight.) Nickel and tungsten on a porous basis, the atomic ratio of tungsten to nickel being from O, 1: 1 to 5: 1 (in the preferred embodiment, from 0.3: 1 to). Catalysts of group U1 and group U111 may contain promoters in amounts not exceeding 8 wt. in a preferred embodiment, not more than 5 wt. t. The best promoters are the elements of groups 11 and IV. The most effective of them are Ti, Zr, Sr, Mg, Zn and Sn type A catalysts may contain molybdenum in usual amounts, i.e. from 2 to 25 weight. molybdenum relative to the total weight of the catalyst, including the porous base. When using less than 2 wt. molybdenum activity is reduced. The molybdenum content exceeding 25 ppm can be used, the activity does not increase, and the cost increases. The amount of metals in the iron group in catalysts A and B may vary depending on the proportions indicated. However, it is preferable to use in the catalysts A two metals of the iron group, each with an atomic ratio to molybdenum of from 0.1 to 0.2. All metals of the iron group may be present, but it is preferable to use two. If a promoter of group IV is used, then only one metal of the iron group is used. The content of the hydrogenating component may be from 0.5 to 40 wt. of the total catalyst, the porosity is porous, but is usually in the range of 2 to 30% by weight. When using a catalyst of type a) it is preferable to choose the content of molybdenum in the range from 4 to 1 5 weight. Z, preferably about 8 wt. % from 0.2 to 10 weight .; Nickel, preferably about 0.5 wtD and from 0.5 to 5 weight. cobalt, preferably about 1.0 wt. If a catalyst of type b is used, it is advisable to choose a tungsten content in the range from 15 to 25 weight (for example, about 19 wt. 2;) and from 2 to 10 wt.% (for example, 6 weight. nickel deposited on a porous substrate, for example, from Okosi aluminum. Trichlorotrifluoroethane used in the system has the following physical properties: Molecular weight T.p. at atmospheres 7,6 at a pressure of 35 ° C Freezing point, 1 ° C Critical temperature 33.7 Critical pressure atm 1,565 g / cm Density at 25 С Viscosity at 21, 0,69 сП Superficial nat 19.25 dyn / s at 25C Trichlorotrifluoroethane is mixed with coal dilution products containing solid particles with a diameter of 0.1-70.0 microns (preferably 0.3.0.0 microns) in a volume ratio of 0.5: 5: 1, preferably 1: 1 - 3: 1 at any temperature, preferably at room and at any appropriate pressure, preferably at atmospheric, for a period of time 0, mun 90 s, preferably 1-30 minutes. After this time has elapsed, the marked phase separation with bottom phase containing coal dilution products, and upper degapodobn In the second phase, there are solid particles whose size is many times larger than the size of the original particles. These phases can be separated by filtration and distillation, very fast filtration, centrifugation, etc. The solvent is easily separated by distillation and recycled with minimal energy consumption due to its low latent heat of vaporization, Example. Coal slurry containing 16.8 kg of crushed Bighorn coal, 27 kg of anthracene oil and 1.6 kg of crushed hydrogenation catalyst, including, weight: Ni 3.8, Mo 10, l, deposited on a substrate from together with 2b , 5 m of alumina, wasp hydrogenation is subjected at 398.88 ° C and a pressure of 27 kg / cm for 0.75 hour. The result is a liquefaction coal product containing 10.9 kg of liquid coal, 13.2 kg of tar and 2.8 kg of solid particles. 27.2 kg of trichlorotrifluoroethane is added to the carbon dilution product. The resulting mixture is stirred for 5 minutes. The mixture is then allowed to separate into an upper phase containing tar, solid particles in some amount of captured trichlorotrifluoroethane, and a lower phase containing liquid coal and Trichlorotrifluoroethane. After separation of the two phases, there is essentially no tar or solid particles in the lower phase. The generalized results of the process are as follows: Coal suspension is used (full weight 5, kg), including, kg: Ighorn coal 1b, 8 Anthracene oil 27.0 Ground hydrotreating catalyst 1.6 Half the recovered recovered oils (full weight 10.9 kg) , including, kg: Saturated hydrocarbons 0, Aromatic hydrocarbon - 0,. Resin7,885 Asphaltenes 2,525
    Insoluble tar and solid particles (total weight 16, OA kg), including, kg:
    Tar13 2
    Particulate matter2.8
    权利要求:
    Claims (1)
    [1]
    1. Patent, GDR No. 180328, cl. 120 1/05, 1975 (prototype).
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    同族专利:
    公开号 | 公开日
    GB2041399B|1982-11-17|
    GB2041399A|1980-09-10|
    BR7806715A|1979-05-08|
    DE2857226A1|1980-05-08|
    EP0001676A2|1979-05-02|
    NL7815043A|1979-10-31|
    CA1100898A|1981-05-12|
    JPS5470302A|1979-06-06|
    AU3957878A|1980-03-13|
    ZA785240B|1979-08-29|
    US4148716A|1979-04-10|
    CS207723B2|1981-08-31|
    FR2433042A1|1980-03-07|
    DD139724A5|1980-01-16|
    EP0001676A3|1979-05-16|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    GB475723A|1935-05-23|1937-11-24|Edeleanu Gmbh|Improvements relating to the refining of hydrocarbon oils|
    US2223184A|1936-08-15|1940-11-26|William E Currie|Splitting up of extracts obtained from solid carbonaceous materials|
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    US4012314A|1975-09-05|1977-03-15|Battelle Memorial Institute|Treating coal liquefaction product oil|US4257869A|1979-08-17|1981-03-24|Electric Power Research Institute|Liquefaction of acid treated coal|
    US4326948A|1980-08-18|1982-04-27|Texaco Inc.|Coal liquefaction|
    JPS6144915B2|1981-05-29|1986-10-04|Kureha Kagaku Kogyo Kk|
    DE3215102A1|1982-04-23|1983-10-27|Joachim A. Dr.-Ing. 6636 Schwalbach Wilhelm|Process for liquefying coal|
    JPH0676585B2|1982-12-28|1994-09-28|三菱化成株式会社|Hydrogenation method of solvent refined coal|
    DE69026645T2|1989-06-05|1996-11-28|Daikin Ind Ltd|Use of foamable compositions|
    EP3103858A1|2015-06-08|2016-12-14|L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude|Method for washing organic liquids with a liquid comprising flurohydrocarbons|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/844,455|US4148716A|1977-10-21|1977-10-21|Process for separating tar and solids from coal liquefaction products using a halogenated aliphatic solvent|
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