Hydrogenation purification method of boil-off gas of phenol-containing and / or aromatic hydrocarbon-containing sewage

Abstract

The invention relates to a hydrogenation purification method for boil-off gas of phenol-containing and / or aromatic hydrocarbon-containing sewage, which is suitable for direct liquefaction of converted coal to produce phenol-containing and aromatic hydrocarbon-containing sewage, can form a combined method of a hydrogenation modification reaction process and a hydrogenation purification reaction process, and can solve the problem that most or all of the phenol-containing and aromatic hydrocarbon-containing sewage produced by direct liquefaction of coal is difficult to biochemically treat. Hydrogenation modification reaction effluent is separated into hot high-pressure separation gas and hot high-pressure separation oil in the hot high-pressure separation process, phenol-containing sewage makes contact with the hot high-pressure separation gas to complete the evaporation process, water-rich gas containing phenol and aromatic hydrocarbon, first gas rich in hydrogen and commonly-existing dust-containing condensate oil are obtained, the first gas is washed by washing oil and subjected to dust falling, and then the second gas becomes second gas; the second gas with the operation temperature higher than the dew point is subjected to a hydrogenation purification reaction process to complete an organic matter deep hydrofining reaction to be converted into a hydrogenation purification reaction effluent with low organic pollutant content, the hydrogenation purification reaction effluent and the quenching material flow are mixed and cooled to the temperature below the dew point, and then cold high-pressure separated water is separated out.

Description

Technical Field

[0001] The present invention relates to a method for hydrogenating and purifying the evaporated gas of wastewater containing phenol and / or aromatic hydrocarbons, which can constitute a combined method of a hydrocarbon hydrogenation reaction process and a hydrogenation purification reaction process of the evaporated gas of phenol-containing wastewater, and is suitable for purifying wastewater containing phenol and aromatic hydrocarbons produced by direct coal liquefaction, and can constitute a combined method of a hydrogenation modification reaction process and a hydrogenation purification reaction process, and can eliminate the problem of difficulty in biochemical treatment of most to all of the wastewater containing phenol and aromatic hydrocarbons produced by direct coal liquefaction. Background Art

[0002] Document A01: ① Publication name: "Coal Direct Liquefaction Technology and Engineering", pages 767 to 768; ② Book code for retrieval: ISBN code: 9-78703-04308-23; ③ Edited by: Wu Xiuzhang, Shu Geping, Li Kejian, Xie Shunmin; ④ Publisher: Science Press, which describes in detail the composition of coal direct liquefaction and hydrogenation modified acidic water and some biochemical treatment methods.

[0003] Table 1 is the analysis results of acidic water from coal direct liquefaction and hydrogenation modification of China Shenhua Ordos Coal-to-Liquids Branch, and Table 2 is a statistical table of the sources, quantities and pollutants of acidic water from coal hydrogenation direct liquefaction unit of China Shenhua Ordos Coal-to-Liquids Branch. The data comes from document A01 "Coal Direct Liquefaction Technology and Engineering", pages 767 to 768. From Tables 1 and 2, it can be seen that the characteristics of organic pollutants in acidic water from coal direct liquefaction and hydrogenation modification are: from the perspective of recovering pure water, all other components are pollutants. The pollutants contain a variety of organic impurities and cannot be treated by a single biochemical method. If a biochemical method is selected to treat organic matter, a combination of multiple biochemical processes with different functions is required, and phenols and aromatic hydrocarbons with more than 2 rings are difficult to be digested and transformed by bacteria. In addition, the presence of chloride ions and metal ions will inevitably lead to a complex process and low efficiency of the biochemical treatment method.

[0004] Table 3 shows the concentration limits of some metals, inorganic substances and organic substances that inhibit nitrification in high-concentration wastewater from coal liquefaction disclosed in document A02. Document A02: ① Publication name: Shenhua Science and Technology (published in September 2016, Vol. 14, No. 5), pages 72 to 76; ② Article name: Experimental study on the effect of BAF method on nitrification reaction of high-concentration wastewater from coal liquefaction; ③ Author: Su Zhiqiang. This document describes the experimental study on the effect of BAF method on nitrification reaction of high-concentration wastewater from coal direct liquefaction project of Shenhua Coal Direct Liquefaction, and describes the concentration limits of some inhibitors that have a strong inhibitory effect on nitrifying bacteria. Once the inhibitor content reaches the concentration listed in Table 3 (the concentration threshold value is very low), it will be toxic or strongly inhibitive to nitrifying bacteria, terminating the expected nitrification reaction of high-concentration wastewater from coal liquefaction, indicating that a small amount of special pollutants can seriously inhibit the biochemical reaction, that is, a slight fluctuation of these special pollutants can seriously affect the effect of the biochemical reaction.

[0005] Take the high-concentration wastewater from coal liquefaction shown in Table 1 as an example. It contains multiple pollutants. Since no single bacterium can digest so many pollutants at the same time, the use of biochemical treatment processes will inevitably lead to the use of multiple biochemical bacteria in series, such as document A03: ① Publication name: "Coal Engineering" (published in 2017, Volume 49, Issue 5), pages 72 to 76; ② Article name: Development and Application of Coal Direct Liquefaction High-concentration Wastewater Treatment Technology; ③ Author: Fan Shujun, Yu Liangyong, Liu Chunhui. This document describes the high-concentration wastewater treatment system of the Shenhua coal direct liquefaction project, which adopts the combined technology of "double-tower stripping + phenol recovery + high-efficiency catalytic oxidation pretreatment + fixed high-efficiency aerated biological filter + ozone oxidation + membrane bioreactor technology + ultrafiltration + reverse osmosis". The disadvantages of this technology are "complex process path, large fluctuation range of operation effect, and large footprint. , large investment"; at the same time, in order to improve the efficiency of deoiling and de-coal powder, demulsifiers are added, in order to increase the deammoniation rate, alkali is added to adjust the pH value of water, and extractants are added to recover phenols. In order to meet the normal survival of bacteria, a variety of other treatment processes for protecting the normal survival of bacteria are adopted and foreign chemicals are added: acids and alkalis are added to adjust the pH value, coagulants such as polyaluminum or polyacrylamide are added in the flotation process, hydroxyl oxidants are used to destroy the aromatic ring structure, bacterial nutrients such as carbon sources are added, ozone is used to destroy the structure of polycyclic aromatic hydrocarbons and new organic species such as quinones are generated, and the activated carbon adsorbent used remains in the water. Adding these foreign materials is essentially adding new pollutant species to the water, which will inevitably result in inefficient conversion of the biochemical conversion process and a variety of non-intrinsic purification demand processes, resulting in too many serial links in the purification process of high-concentration sewage from coal liquefaction and unstable conversion effect.

[0006] Table 1 Analysis results of acidic water from coal direct liquefaction and hydrogenation modification of China Shenhua Ordos Coal-to-Liquids Branch (unit: mg / L, except pH)

[0007]

[0008] Table 2 Statistics of sources, quantities and pollutants of acidic water in the coal hydroprocessing direct liquefaction unit of China Shenhua Ordos Coal-to-Oil Branch

[0009]

[0010] Table 3 Concentration limits of some metals, inorganic substances and organic substances that inhibit nitrification in high-concentration wastewater from coal liquefaction disclosed in document A02

[0011]

[0012] However, by analyzing the data in Table 1 and Table 2, it can be seen that the pollutants in the acidic water of coal direct liquefaction and hydrogenation modification have the following characteristics: From the perspective of recovering pure water, in 86.5t / h of sewage, the amount of volatile phenols is 486.8kg / h (accounting for 0.563% by weight), and the amount of oil is 1912.5kg / h (accounting for 2.211% by weight). Considering the biochemical purification, the amount is huge, but if the hydrogenation purification is considered, the absolute amount of its reaction task is very small, and a single reaction process can convert all organic matter and toxic inorganic matter, which can achieve the ideal goal of deep purification of simple process. Table 6 is the first sewage (desulfurization and hydrogen removal of high-concentration sewage from coal liquefaction) The pollutant composition table of pretreated wastewater after ammonia and before dephenolization, the data in Table 6 more strongly supports the above view; the hydrogenation conversion of wastewater can naturally achieve the separation of solid and evaporation components, but requires the liquid phase to carry and wash solids to prevent solid accumulation and clogging the flow channel; the hydrogenation conversion of wastewater requires that the wastewater is best gasified into water-dry gas, so the heat consumed by wastewater gasification needs to be recovered at a high ratio to reduce energy consumption; of course, in order to reduce the difficulty of direct coal liquefaction and hydrogenation modification acidic water hydrogenation purification reaction, it is best to pretreat the raw wastewater first: remove solids, remove free oil, remove hydrogen sulfide, remove carbon dioxide, remove ammonia, remove phenols, and remove high-boiling hydrocarbons. One or more of the following.

[0013] Since chloride ions and fluoride ions interact strongly with water molecules or hydrogen ions in water molecules, the step of removing chloride ions and fluoride ions (such as reverse osmosis step) is usually the last step to remove pollutants in direct coal liquefaction and hydrogenation modification of acidic water, and all steps before this are pretreatment steps for the step of removing chloride ions and fluoride ions. A large part of the polluting components such as hydrogen sulfide, ammonia and carbon dioxide can be removed by the process of stripping evaporation fractionation tower. In this way, the main targets of the biochemical treatment step are hydrocarbon oils such as phenols, dicyclic aromatic hydrocarbons, polycyclic aromatic hydrocarbons, and other trace components coexisting in the wastewater of the biochemical treatment step. They are both target components of bacterial biochemical treatment and poisons of bacteria.

[0014] For organic heteroatom hydrocarbons (especially organic heteroatom aromatic hydrocarbons) in sewage, the purification of water components is essentially the process of eliminating or greatly reducing the electrical conductivity of organic heteroatom hydrocarbons (especially organic heteroatom aromatic hydrocarbons), because only in this way can the interaction between organic heteroatom hydrocarbons (especially organic heteroatom aromatic hydrocarbons) and water molecules be eliminated, that is, it is necessary to remove heteroatoms and destroy the benzene ring structure. However, in the biochemical process of hydrocarbons containing organic oxygen, organic nitrogen, organic sulfur, and organic metals, the long carbon-carbon bond chain is broken into short carbon chain molecules or even single carbon atom molecules such as methane and carbon dioxide, and the organic oxygen atoms are converted into small molecules such as water and carbon dioxide. Molecular substances, organic nitrogen atoms are converted into small molecular substances such as nitrogen and ammonia, and organic sulfur atoms are converted into small molecular substances such as hydrogen sulfide and sulfur dioxide. It can be seen that a large number of carbon-carbon bond breaking reactions and carbon-heteroatom bond breaking reactions occur. Therefore, it belongs to a large change process of chemical reaction tasks, and because biochemical processes usually occur at room temperature and cannot use high temperature means, a commonly used and effective chemical bond breaking condition, its reaction efficiency is extremely low, and the toxic components can only start the digestion reaction after being absorbed into the body by bacteria. Therefore, the reaction selectivity is very low, resulting in a long biochemical reaction time, low efficiency, and a huge system; in addition, the reuse value of the biochemical products of organic heteroatom hydrocarbons is extremely low.

[0015] In the biochemical process of hydrocarbons containing organic oxygen, organic nitrogen, organic sulfur, and organic metals, the long chain carbon-carbon bonds are broken into short-chain molecules or even single-carbon atom molecules such as methane and carbon dioxide, organic oxygen atoms are converted into small molecules such as water and carbon dioxide, organic nitrogen atoms are converted into small molecules or ionic groups such as nitrogen and nitro, and organic sulfur atoms are converted into small molecules such as hydrogen sulfide and sulfur dioxide. It can be seen that a large number of carbon-carbon bond breaking reactions and carbon-heterobond breaking reactions occur. On the other hand, for organic matter mainly composed of carbon and hydrogen elements, the effect of sewage biochemical treatment can be mainly classified as an electrical elimination reaction, that is, the electrical elements are separated from carbon and hydrogen elements or the carbon-carbon unsaturated bonds are deeply saturated.

[0016] Heteroatom organic matter and aromatic hydrocarbons in sewage are all organic matter with electron donors.

[0017] Compared with the sewage purification goal, the hydrogenation conversion process of deep hydrogenation refining reaction can eliminate or significantly reduce the electronegativity of organic heteroatom hydrocarbons (especially organic heteroatom aromatics) in sewage, and has the following characteristics: the hydrogenation refining catalyst has the ability to selectively adsorb and react to pollutants with electronegativity, thereby having high reaction efficiency and high impurity removal rate, and the number of reactions in which the carbon-carbon bond breaks can be very small, that is, the carbon-carbon bond length is maintained as much as possible, thereby increasing the use value of the carbon-carbon bond group. Therefore, from the above perspective, the deep hydrogenation refining reaction purification method of sewage has higher purification efficiency, higher removal rate and higher value of the purified product.

[0018] For the purification goal of high-concentration wastewater from direct coal liquefaction, based on the characteristics that almost all impurity elements contained in these pollutants can be almost completely hydrogenated and converted in the deep hydrogenation refining process, and all kinds of unsaturated chemical bonds contained can be deeply hydrogenated and saturated in the deep hydrogenation refining process, the present invention believes that high-concentration wastewater from direct coal liquefaction (preferably phenol-containing and aromatics-containing wastewater after pretreatment) is converted into dry gas of water, and then purified through a deep hydrogenation purification process. The biochemical treatment characteristics of the final cold high-separation water can be close to or equivalent to the easy biochemical treatment characteristics of hydrogenated cold high-separation water.

[0019] Water-dry gas refers to the gas whose operating temperature is higher than the dew point temperature of water and there is no liquid water in the gas.

[0020] Water-wet gas refers to a gas whose operating temperature is lower than the dew point temperature of water and contains liquid water.

[0021] The hydrogenation purification of high-concentration sewage from direct coal liquefaction requires that the sewage entering the hydrogenation purification reaction process is in the gas phase and preferably in the water-dry state. This is because the suitable hydrogenation purification catalyst reaction conditions for the hydrogenation purification reaction of pollutants usually require a certain hydrogen partial pressure, a relatively high reaction temperature, and the presence of hydrogen sulfide. If the main water is liquid, the following main problems exist: ① The water phase dissolves hydrogen sulfide, hydrogen chloride, and hydrogen fluoride to become acidic substances, corroding the catalyst, reactor internals, and reactor walls; ② The water phase soaks the hydrogenation purification catalyst, weakening its structural strength and pulverizing it; ③ The liquid water vaporizes and absorbs a large amount of heat, which will lower the reaction temperature; ④ The hydrogenation purification catalyst The liquid water adsorbed by the catalyst vaporizes and expands violently, which may burst and shatter the hydrogenation purification catalyst. Therefore, the operating temperature of the hydrogenation purification reaction feed, the hydrogenation purification reaction process, and the hydrogenation purification reaction product is usually as far higher than the water dew point temperature of the reaction material as possible. When the operating temperature of the hydrogenation purification reaction product is close to or lower than the dew point temperature, it is usually made to enter a water phase state in which there are suitable alkaline substances such as ammonia molecules that can neutralize acidic substances such as hydrogen sulfide, hydrogen chloride, and hydrogen fluoride through a rapid cooling process. These alkaline substances such as ammonia molecules can be products of the hydrogenation purification reaction and / or products of the hydrocarbon hydrogenation reaction process R1 and / or substances injected from the outside.

[0022] In order to reduce the energy consumption of the hydrogenation purification process of high-concentration wastewater from direct coal liquefaction, it is necessary to ensure that the recovery rate of the heat absorbed during the vaporization process of high-concentration wastewater from direct coal liquefaction (latent heat of water evaporation) is at a high level, such as higher than 75-85%. Due to the strong hydrogen bonds between liquid water molecules, as the temperature drops, the collective attraction between water molecules increases rapidly, and the saturated vapor pressure of liquid water drops rapidly. This characteristic of water just provides this possibility.

[0023] Table 4 shows the saturated vapor pressure of water at 20-250°C and the water condensation ratio of the condensation process of water saturated gas at 250°C.

[0024] It can be seen from Table 4 that for a total pressure of 170 kg / cm 2 A. For water-saturated gas at a temperature of 250°C, when the condensation process reaches the conventional temperature condition of 160°C that can be achieved by the heat recovery heat exchanger, the water condensation ratio reaches 84.46%, which means that approximately 84.46% of the total latent heat of the total water component in the water-saturated gas at 250°C is recovered.

[0025] Table 4 uses a total pressure of 170 kg / cm 2 A. The water condensation ratio of the condensation process of water-saturated gas at a temperature of 250°C is used to illustrate the problem because this is close to the normal operating conditions. If the total pressure is 170kg / cm 2 A. Water-saturated gas with a temperature of 275°C, the saturated water content will increase by an astonishing 49.56%. Therefore, the present invention has a huge room for improving the amount of high-concentration wastewater treated by direct coal liquefaction. Of course, the saturated volume concentration of the water component is increased from 23.86 volume % to 35.682 volume %, and the hydrogen partial pressure will decrease. This also shows that: by reducing the number of macromolecules in the R2 feed of the hydrogenation purification reaction process to reduce the reaction hydrogen partial pressure value required for organic matter, the amount of high-concentration wastewater treated by direct coal liquefaction can be greatly increased.

[0026] In order to reduce the investment and energy consumption of the hydrogenation purification system of the evaporated gas of the phenol-containing and aromatic hydrocarbon wastewater produced by direct coal liquefaction, it is necessary to reduce the number of special systems, that is, it is necessary to construct a method for combining the hydrocarbon hydrogenation reaction process with the hydrogenation purification reaction process of the evaporated gas of the phenol-containing wastewater. For example, a method for combining the hydrogenation modification reaction process with the hydrogenation purification reaction process can be constructed, and the hydrogen, hydrocarbon oil gas, temperature and pressure conditions in the hot high-fraction gas separated from the hydrogenation modification reaction product are used to first spray it into the wastewater to realize wastewater gasification. At the same time, the hot high-fraction gas of the hydrogenation modification reaction product is cooled to produce condensed oil, which washes the gas, rinses the solid, and absorbs the macromolecular phenols and macromolecular hydrocarbons in the feed of the hydrogenation purification reaction process to form a condensate in the wastewater vaporization process. In this way, the boiling point and amount of the external washing oil in the special oil washing step can be reduced, and the condensate containing solids, high-boiling-point phenols and macromolecular aromatics obtained in the wastewater gasification process enters a system capable of treating solid hydrocarbon materials for treatment. Classified recycling: for example, the hot high-fraction oil of the hydrogenation modification reaction product enters the separation and distillation process FRAC80 to be separated into narrow fraction oils of different boiling ranges, and the solid particles enter the separation bottom oil FRAC80-DV with the highest boiling point in the separation and distillation process FRAC80. Usually, the separation bottom oil FRAC80-DV is used as a solvent oil to prepare the oil-coal slurry for use as a raw material for coal hydrogenation direct liquefaction reaction. In this way, the high-boiling point pollutant components (solids, macromolecular phenols, macromolecular hydrocarbons) from the sewage contained in the condensate are finally classified and recycled as products of the "coal hydrogenation direct liquefaction reaction fractionation system", eliminating the problems of biochemical conversion and hydrogenation purification of these pollutant components. Therefore, the method of the present invention is an optimization technology for the overall process properties of sewage, which realizes the effect of "hydrogenation conversion of low-boiling point organic components, fractionation of high-boiling point organic components, and return of solid components to the coal hydrogenation direct liquefaction reaction fractionation system and finally entering the liquefied residue".

[0027] Table 4 Saturated vapor pressure of water at 20-250℃, water condensation ratio during condensation of saturated water at 250℃

[0028]

[0029]

[0030] When the hydrocarbon hydrogenation reaction process R1 performs a hydrogenation modification reaction process, the hydrogenation modification reaction process R1 is combined with the hydrogenation purification reaction process R2, which has the following advantages:

[0031] ① The reaction effluent R1P of the hydrogenation modification reaction process is a logistics containing phenol, aromatics, water and hydrogen. Its hot high-fraction gas or de-oiled hot high-fraction gas undergoes a hydrogenation purification reaction process, and at the same time, the pollutants such as phenol and aromatics are purified, so that the condensate of the water component in the hydrogenation modification reaction effluent R1P is purified, reducing the output of phenol-containing and aromatics-containing wastewater;

[0032] According to conventional processes, when the reaction effluent R1P of the hydrogenation modification reaction process is condensed and separated separately, clean washing water needs to be added to prevent the crystals such as sulfhydrylamine and ammonium chloride from precipitating and blocking the flow channel, thereby generating more phenol-containing and aromatic wastewater;

[0033] ② The phenol- and aromatic-containing wastewater from the direct liquefaction product of coal hydrogenation exists in the effluent of the hydrogenation purification reaction after the hydrogenation purification reaction process. It is used as washing water for the second time in the quenching process to prevent the deposition of crystals such as amine sulfhydride and ammonium chloride from blocking the flow channel, thereby saving the clean washing water input from the outside and reducing the overall acidic water production;

[0034] ③ In essence, the liquid phenol- and aromatic-containing wastewater from the direct liquefaction product of coal hydrogenation, after the vaporization process, belongs to the same type of substance as the water component (coexisting with the phenol component and the aromatic component) in the hydrogenation modification reaction effluent R1P, and the hot high-pressure separation process of the hydrogenation modification reaction effluent R1P belongs to the separation process of removing heavy aromatic components and possible solid particles, and part of the hydrocarbon oil contained in the hot high-fraction gas R1P-S1V of the hydrogenation modification reaction effluent R1P can be used as a gas phase washing oil in the cooling and condensing process of the vaporization process of the first wastewater, which adheres to and carries the solid particles in the gas phase to achieve the purification effect of removing the solid particles.

[0035] The phenol-containing and aromatics-containing wastewater produced by direct coal liquefaction is subjected to the hydrogenation purification conversion reaction process of the present invention to obtain cold high-grade acidic water KSW. The treatment process of cold high-grade acidic water KSW01 can be any appropriate method, for example, it can be the same treatment method as the hydrogenation-modified acidic water, that is, after filtration, deoiling, and removal of dissolved gas, after the acidic water stripping process U700 dehydrogen sulfide and deammoniation process, preliminary purified water KSW05 containing chloride ions and fluoride ions is obtained, and then the preliminary purified water KSW05 is subjected to simple biochemical treatment, ultrafiltration, and reverse osmosis processes to obtain qualified purified water KSW08, which can replace fresh water or desalted water.

[0036] So far, the basic concept of the present invention has been proposed.

[0037] The basic concept of the present invention is: a hydrogenation purification method for the evaporated gas of wastewater containing phenol and / or aromatics, which can constitute a combined method of a hydrocarbon hydrogenation reaction process and a hydrogenation purification reaction process of the evaporated gas of phenol-containing wastewater, is suitable for converting phenol-containing and aromatics-containing wastewater produced by direct coal liquefaction, and can constitute a combined method of a hydrogenation modification reaction process and a hydrogenation purification reaction process, which can eliminate the problem of the difficulty in biochemical treatment of most to all of the phenol-containing and aromatics-containing wastewater produced by direct coal liquefaction. The hydrogenation modification reaction effluent is separated into hot high-fraction gas and hot high-fraction oil in a hot high-pressure separation process. The phenol-containing wastewater is contacted with the hot high-fraction gas to complete the evaporation process to obtain a first gas rich in water and hydrogen containing phenol and aromatics, and dust-containing condensed oil that is usually present. The first gas is washed and dusted by washing oil to become a second gas. The second gas, whose operating temperature is higher than the dew point, is converted into a hydrogenation purification reaction effluent with a low organic pollutant content after completing a deep hydrogenation refining reaction of organic matter through a hydrogenation purification reaction process and is mixed with a quenching logistics to cool to a temperature below the dew point to separate the cold high-fraction water.

[0038] In a broad sense, the present invention belongs to a method for separating phenol-containing and aromatic hydrocarbon-containing wastewater by chemical reaction.

[0039] As described above, the basic concept of the present invention is: first, wastewater is gasified to obtain dry gas, and then the dry gas is subjected to a deep hydrogenation purification reaction to obtain a clean water gas flow. Of course, in order to ensure the continuous and stable operation of the "dry gas deep hydrogenation purification reaction", coal direct liquefaction high-concentration wastewater needs to be pretreated before gasification, such as removing solids (ash, unliquefied coal, etc.), deoiling, dehydrogen sulfide, deammoniation, phenol recovery, preheating, pressurization and other steps or several of the above. Before the dry gas enters the hydrogenation purification reaction process, it needs to be oil washed to remove solid dust and cooled to separate high-boiling hydrocarbons and high-boiling phenol.

[0040] The hydrogenation purification of evaporated gas from phenol-containing and aromatic hydrocarbon-containing wastewater described in the present invention refers to a process in which organic and inorganic substances in the phenol-containing and aromatic hydrocarbon-containing wastewater are converted into deep purification by conventional processes through a hydrogenation purification reaction process, especially reducing the difficulty of the biochemical treatment process. The main characteristics are that it has one or more of the following characteristics: converting heteroatoms in organic matter into inorganic matter, converting organic matter with high hydrogen unsaturation into organic matter with high hydrogen saturation to reduce its electrical conductivity and reduce its biochemical toxicity, converting difficult-to-separate inorganic matter into easily-separated inorganic matter, and reducing the solubility of hydrocarbons in water.

[0041] Traditional biochemical treatment methods directly introduce a variety of organic substances that are difficult for bacteria to digest in the biochemical process of coal liquefaction and high-concentration wastewater, such as organic oxides (phenols, etc.), organic nitrogen compounds, organic sulfides, cyanides, organic chlorides, organic fluorides, dicyclic aromatic hydrocarbons, polycyclic aromatic hydrocarbons, and organic metal compounds, into the biochemical process, which inevitably results in an inefficient and complex process.

[0042] If the wastewater gasification and solid removal method is carried out at a relatively low operating pressure, the volume of the wastewater evaporated gas is too large, resulting in a significant increase in the spatial entropy of the solid particles (i.e., they are dispersed in a huge space), and a huge amount of washing oil is required to wash such highly dispersed solid particles. The method of the present invention, especially the combined process formed with the hydrogenation reaction process R1, simply realizes the condition of high water vapor partial pressure, thereby greatly reducing the operating volume of the wastewater evaporated gas, reducing the dispersion of the solid particles, and can greatly reduce the washing oil. The hydrocarbon oil in the process logistics can be used as the washing oil, and the washing oil that adsorbs the solid particles enters the distillation system for jointly treating other hydrocarbon oils containing solid particles, thereby simplifying the overall process.

[0043] In comparison, the present invention believes that the fundamental reason why the existing coal direct liquefaction high-concentration wastewater organic matter treatment process is complicated and inefficient is that: due to the failure to discover the advantages of the hydrogenation method, the light oil wastewater biochemical treatment path model of the petroleum industry is followed, and the coal direct liquefaction high-concentration wastewater that is difficult to simply and efficiently treat biochemically is "assumed to be" raw wastewater suitable for biochemical treatment for treatment, which will inevitably lead to the inherent logical defects of the process path characteristics: a variety of organic substances in the coal direct liquefaction high-concentration wastewater that are difficult to be digested by bacteria in the biochemical process, such as organic oxides (phenols, etc.), organic nitrogen compounds, organic sulfides, cyanides, organic chlorides, organic fluorides, dicyclic aromatic hydrocarbons, polycyclic aromatic hydrocarbons, and organic metal compounds are directly introduced into the biochemical process, which will inevitably result in inefficient conversion of the biochemical conversion process and complex serial application of multiple processes, and unstable conversion effect.

[0044] Compared with the treatment method for phenol-containing and aromatic hydrocarbon-containing wastewater produced by direct coal liquefaction described in document A03, the gasification hydrogenation method for phenol-containing wastewater of the present invention utilizes the strong adsorption force of the hydrogenation refining catalyst on the pollutant-electrolyzing body to improve the reaction selectivity and the depth of the purification reaction. Under the conditions of high hydrogen partial pressure and low liquid hourly space velocity, it has the effect of deeply converting multiple pollutants in a single conversion step. Therefore, the process is simple and the conversion efficiency is high. When combined with the hydrocarbon hydrogenation reaction process, the investment and energy consumption are low. Therefore, it has significant technical advantages and is a new method that functionally replaces the biochemical treatment process.

[0045] The evaporation method of the phenol-containing and aromatic hydrocarbon-containing wastewater used in the present invention can be any reasonable method, for example, the phenol-containing and aromatic hydrocarbon-containing wastewater can first absorb heat and evaporate into saturated water vapor, and then mix with hydrogen-containing gas to form dry gas of water; the phenol-containing and aromatic hydrocarbon-containing wastewater can be preheated and then sprayed into high-temperature hydrogen-containing gas to evaporate and mix into the gas phase to form dry gas of water; it can be the above-mentioned mixing process; the number of nozzles for spraying the phenol-containing and aromatic hydrocarbon-containing wastewater into the high-temperature hydrogen-containing gas can be 1, 2 or more injection points.

[0046] The hydrogenation purification reaction process of the present invention can set up multiple sub-reaction zones using hydrogenation purification catalysts, adopt a parallel branch reaction zone switching working mode, or adopt a series sub-reaction zone receiving fresh sewage gas raw materials in time periods to extend the continuous operation cycle.

[0047] By extension, the present invention can treat phenol-containing and / or aromatic hydrocarbon-containing wastewater from various sources. Depending on the source, the present invention can simultaneously treat part or all of the following "organic components that can be detoxified by hydrogenation purification reaction":

[0048] ① Organic matter containing heteroatoms, which can be oxygen, nitrogen, sulfur, or metal atoms;

[0049] Oxygen-containing organic matter, including one or more of phenol, aldehyde, alcohol, ether, ketone, dibenzofuran, and carboxylic acid;

[0050] Sulfur-containing organic matter, including one or more of thiophenol, mercaptan, thioether, thiophene, thionaphthene and dithiothrene;

[0051] Nitrogen-containing organic substances, including one or more of nitrile, isocyanide, amide, pyrrole, pyridine, aniline, indole, organic cyanide, quinoline, carbazole, acridine, acrylene, fluoranthene, azafluorene, and azacarbazole;

[0052] The heteroatom metal atom can be nickel, vanadium, iron, copper, aluminum, lead, etc.;

[0053] Extractants for phenols;

[0054] ②Inorganic substances, hydrogen cyanide, carbon monoxide, carbon dioxide, etc.

[0055] The present invention is suitable for newly-built devices or for the transformation of existing devices.

[0056] The method of the present invention has not been reported.

[0057] Therefore, the first object of the present invention is to provide a method for hydrogenating and purifying evaporated gas from wastewater containing phenol and / or aromatic hydrocarbons.

[0058] The second object of the present invention is to provide a method for combining a hydrocarbon hydrogenation reaction process with a hydrogenation purification reaction process of evaporated gas from wastewater containing phenol and aromatic hydrocarbons.

[0059] The third object of the present invention is to provide a purification method suitable for phenol- and aromatic-containing wastewater produced by direct coal liquefaction.

[0060] The fourth object of the present invention is to propose a method for combining a hydrogenation modification reaction process with a hydrogenation purification reaction process. Summary of the invention

[0061] The present invention provides a method for hydrogenating and purifying evaporated gas of wastewater containing phenol and / or aromatic hydrocarbons, which is characterized by comprising the following steps:

[0062] The pollutant components KC contained in the first sewage include phenol and / or aromatic hydrocarbons, include or exclude solid particles, and include or exclude other pollutant components that can undergo hydrogenation conversion reactions in the hydrogenation purification reaction process R2 to reduce their molecular electrical conductivity;

[0063] The heteroatom-containing organic matter includes oxygen-containing organic matter, includes or excludes nitrogen-containing organic matter, includes or excludes sulfur-containing organic matter, includes or excludes chlorine-containing organic matter;

[0064] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0065] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to produce organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to produce aromatic hydrocarbons with a lower aromatic carbon rate.

[0066] The present invention is usually operated as follows:

[0067] ⑴The first source of sewage

[0068] The first sewage, containing or not containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0069] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0070] ⑵ Wastewater gasification process U2

[0071] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0072] The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas;

[0073] The first sewage vaporized gas U2V-1 contains or does not contain liquid hydrocarbon oil;

[0074] ⑶ Hydrogenation purification reaction process R2

[0075] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0076] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0077] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0078] The present invention generally operates in the following manner:

[0079] ⑴The first source of sewage

[0080] The source of the first wastewater includes one or more of the following processes: coal hydrogenation direct liquefaction process, coal gasification process, coal dry distillation process, coal tar processing process;

[0081] The first sewage, containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0082] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal;

[0083] ⑵ Wastewater gasification process U2

[0084] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0085] The first sewage vaporization gas U2V-1 is water dry gas;

[0086] The first sewage vaporized gas U2V-1 contains liquid hydrocarbon oil;

[0087] ⑶ Hydrogenation purification reaction process R2

[0088] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the water-dry stream U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0089] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0090] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0091] The present invention generally operates as follows:

[0092] ⑴The first source of sewage

[0093] The first sewage, containing or not containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0094] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal;

[0095] ⑵ Wastewater gasification process U2

[0096] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0097] The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas;

[0098] The first sewage vaporized gas U2V-1 contains or does not contain liquid hydrocarbon oil;

[0099] ⑶ Hydrocarbon hydrogenation reaction process R1 and hydrogenation purification reaction process R2

[0100] A hydrogen-containing gas phase stream R1P-VB based on the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is subjected to a hydrogenation purification reaction process R2;

[0101] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0102] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0103] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics R1P-VB undergoes a hydrogenation refining purification reaction of at least a portion of the pollutant components to be converted into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0104] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics R1P-VB undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0105] In the hydrogenation purification reaction process R2, the components based on the stream U2V-1B or the intermediate hydrogenation products based on the components of the stream U2V-1B are mixed and contacted with the stream R1P-VB or the intermediate hydrogenation products of the stream R1P-VB;

[0106] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0107] The present invention generally operates as follows:

[0108] ⑴The first source of sewage

[0109] The source of the first wastewater includes one or more of the following processes: coal hydrogenation direct liquefaction process, coal gasification process, coal dry distillation process, coal tar processing process;

[0110] The first sewage, containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0111] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal;

[0112] ⑵ Wastewater gasification process U2

[0113] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0114] The first sewage vaporization gas U2V-1 is water dry gas;

[0115] The first sewage vaporized gas U2V-1 contains liquid hydrocarbon oil;

[0116] ⑶ Hydrocarbon hydrogenation reaction process R1 and hydrogenation purification reaction process R2

[0117] A hydrogen-containing gas phase stream R1P-VB based on the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is subjected to a hydrogenation purification reaction process R2;

[0118] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0119] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0120] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics R1P-VB undergoes a hydrogenation refining purification reaction of at least a portion of the pollutant components to be converted into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0121] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics R1P-VB undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0122] In the hydrogenation purification reaction process R2, the components based on the stream U2V-1B or the intermediate hydrogenation products based on the components of the stream U2V-1B are mixed and contacted with the stream R1P-VB or the intermediate hydrogenation products of the stream R1P-VB;

[0123] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0124] In the present invention, usually, the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is a stream containing phenol, aromatic hydrocarbons, water and hydrogen.

[0125] In the present invention, generally, the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1;

[0126] The logistics based on the hot high-fraction gas R1P-S1V is mixed and contacted with the logistics based on the first sewage to form water-dry or water-wet first sewage vaporized gas U2V-1.

[0127] The present invention, generally, (3) sets a sewage spray gasification process WDV;

[0128] In the sewage spray gasification process WDV, a liquid water-containing logistics based on the first sewage is sprayed into a gas-containing logistics based on the hot high-fraction gas R1P-S1V for vaporization to form a logistics containing water-dry first sewage vaporized gas U2-2. The operating temperature of the water-dry first sewage vaporized gas U2-2 is lower than the operating temperature of the logistics R1P-S1V, with or without the generation of condensed oil WDV-L.

[0129] In the present invention, generally, (3) during the sewage spray gasification process WDV, condensed oil WDV-L is produced;

[0130] Condensate oil WDV-L, with or without solid particles from the first sewage.

[0131] In the present invention, usually, (3) in the wastewater spray gasification process WDV, the condensed oil WDV-L is separated so that it does not undergo the hydrogenation purification reaction process R2.

[0132] In the present invention, usually, (3) in the cold high-pressure separation process S7, the water-containing and hydrogen-containing flow based on the hydrogenation purification reaction effluent R2P is separated to obtain cold high-pressure water separation S7-W.

[0133] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0134] At least a portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrogenation purification reaction effluent R2P for recycling.

[0135] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0136] At least a portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrocarbon hydrogenation reaction process R1 for recycling.

[0137] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0138] A portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrocarbon hydrogenation reaction process R1 for recycling;

[0139] A portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrogenation purification reaction effluent R2P for recycling without passing through the hydrocarbon hydrogenation reaction process R1.

[0140] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0141] The hydrogen concentration in the cold high-fraction gas S7-V is 75 to 98 volume %.

[0142] In the present invention, generally, the reaction index of (3) hydrogenation purification reaction process R2 is as follows:

[0143] The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 80%;

[0144] The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 80%;

[0145] The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 80%;

[0146] In the hydrogenation purification reaction process R2, the hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon reduces the aromatic carbon ratio by more than 60%;

[0147] The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 70%;

[0148] The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%;

[0149] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 35 weight %;

[0150] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 15 weight %;

[0151] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 10 weight %.

[0152] In the present invention, generally, the reaction index of (3) hydrogenation purification reaction process R2 is as follows:

[0153] The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 90%;

[0154] The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 90%;

[0155] The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 90%;

[0156] In the hydrogenation purification reaction process R2, the hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon reduces the aromatic carbon ratio by more than 70%;

[0157] The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%;

[0158] The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 90%;

[0159] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 17.5 weight %;

[0160] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 7.5 weight %;

[0161] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 5.0 weight %.

[0162] The present invention preferably has the following reaction indexes in the (3) hydrogenation purification reaction process R2:

[0163] The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 98%;

[0164] The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 98%;

[0165] The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 98%;

[0166] The hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%;

[0167] The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 90%;

[0168] The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 95%;

[0169] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 9 weight %;

[0170] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 6 weight %;

[0171] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 3 weight %.

[0172] In the present invention, generally, the purification index of (3) hydrogenation purification reaction process R2 is as follows:

[0173] The weight content of organic oxygen in the hydrocarbons in the hydropurification reaction effluent R2P is less than 5 ppm;

[0174] The weight content of organic nitrogen in the hydrocarbons in the hydropurification reaction effluent R2P is less than 5 ppm;

[0175] The organic sulfur content in the hydrocarbons in the hydropurification reaction effluent R2P is less than 2 ppm by weight.

[0176] In the present invention, generally, the purification index of (3) hydrogenation purification reaction process R2 is as follows:

[0177] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 5 weight %;

[0178] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 2 weight %;

[0179] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 1 weight %.

[0180] In the present invention, generally, the operating conditions of the hydrogenation purification reaction process R2 are: pressure of 6 to 25 MPa, temperature of 220 to 440°C, hydrogen to oil ratio of 2000 to 20000 Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.05~10.0h -1 .

[0181] In the present invention, generally, the operating conditions of the hydrogenation purification reaction process R2 are: pressure of 12-20 MPa, temperature of 270-390°C, hydrogen-to-oil ratio of 2000-20000 Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.2~1.0h -1 .

[0182] In the present invention, generally, the raw hydrocarbons in the hydrocarbon hydrogenation reaction process R1 are hydrocarbon materials containing phenols and aromatics, including hydrocarbons with a conventional boiling point higher than 350°C;

[0183] The operating conditions of hydrocarbon hydrogenation process R1 are usually: pressure of 6-25 MPa, temperature of 220-460°C, hydrogen-to-oil ratio of 100-3000 Nm 3 / t;

[0184] The operating conditions of the hydrogenation purification reaction process R2 are usually: pressure of 6-25MPa, temperature of 220-440℃, hydrogen-to-oil ratio of 2000-20000Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.05~10.0h -1 .

[0185] In the present invention, generally, the raw hydrocarbons of the hydrocarbon hydrogenation reaction process R1 are hydrocarbon materials containing phenols and aromatics, including hydrocarbons with a conventional boiling point higher than 350°C;

[0186] The operating conditions of hydrocarbon hydrogenation process R1 are generally: pressure of 12-20 MPa, temperature of 320-440°C, hydrogen-to-oil ratio of 200-2000 Nm 3 / t;

[0187] ⑶ The operating conditions of hydrogenation purification reaction process R2 are generally: pressure of 12-20MPa, temperature of 270-390℃, hydrogen-to-oil ratio of 2000-20000Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.2~1.0h -1 .

[0188] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0189] Cold high-purity water S7-W has a phenol content of less than 10ppm and an aromatic content of less than 200ppm.

[0190] In the present invention, generally, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high fraction gas S7-V, cold high fraction water S7-W, and cold high fraction oil S7-L;

[0191] Cold high-purity water S7-W has a phenol content of less than 5ppm and an aromatic content of less than 50ppm.

[0192] In the present invention, generally, (2) in the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM containing water, phenol and / or aromatic hydrocarbons in the first sewage is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0193] In the first oil washing process U3, the logistics U2V-1VB based on the first sewage vaporized gas U2V-1 contacts the washing oil U3-AL at least once to obtain the first washed gas U3-PV and the first washed oil U3-PL;

[0194] The amount of solids in the first washed gas U3-V is less than the amount of solids in the gas phase of the stream U2V-1VB.

[0195] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0196] At least a part of the stream based on the cold high fraction oil S7-L is recycled as wash oil U3-AL.

[0197] In the present invention, generally, (3) a gas-phase-containing stream R2P-VB based on the hydrogenation purification reaction effluent R2P is mixed with a quenching stream KS and cooled to a temperature below the water dew point to form a mixed-phase material R2P-VB-2 containing a gas phase and a liquid phase;

[0198] The mixed phase material R2P-VB-2 comprises an aqueous phase in which an ammonia component is dissolved.

[0199] In the present invention, usually, (3) the quenching logistics KS is quenching hydrogen-rich gas and / or quenching oil and / or quenching water.

[0200] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0201] The quenching logistics KS is quenching hydrogen-rich gas based on cold high-fraction gas S7-V, and / or quenching oil based on cold high-fraction oil S7-L, and / or quenching water based on cold high-fraction water S7-W.

[0202] In the present invention, generally, (3) the hydrocarbon hydrogenation reaction process R1, the raw hydrocarbon R1F is a distillation oil obtained by separating the oil generated by the direct liquefaction reaction of coal hydrogenation, the hydrocarbon hydrogenation reaction process R1 undergoes a partial hydrogenation saturation reaction of bicyclic aromatic hydrocarbons and / or polycyclic aromatic hydrocarbons, and the hydrogen supply index of the hydrocarbons with a conventional boiling point higher than 200° C. in the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is higher than the hydrogen supply index of the hydrocarbons with a conventional boiling point higher than 200° C. in the raw hydrocarbon R1F;

[0203] The hydrocarbon oil rich in hydrogen-donating hydrocarbon obtained by separating the hydrogenation reaction effluent R1P is used as a hydrogen-donating solvent and prepared with coal powder to form an oil-coal slurry, which is converted into the coal hydrogenation direct liquefaction reaction effluent through a coal hydrogenation direct liquefaction reaction process;

[0204] Separating the effluent from the direct liquefaction reaction of coal hydroprocessing to obtain a distillate oil based on the oil produced by the direct liquefaction of coal hydroprocessing, and using it as the feedstock oil R1F of the hydrocarbon hydrogenation reaction process R1;

[0205] The process of separating the effluent from the direct liquefaction reaction of coal hydroprocessing obtains the initial phenol-containing and aromatic-containing wastewater;

[0206] Based on the initial phenol-containing and aromatic-containing wastewater, the first wastewater is obtained.

[0207] The present invention, usually, (1) the first sewage source

[0208] The first sewage, with or without solid particles, is sewage that has undergone a sewage pretreatment process;

[0209] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal.

[0210] In the present invention, usually, (i) the first sewage is an aqueous solution containing phenol and aromatic hydrocarbons and contains chloride ions and / or fluoride ions.

[0211] The present invention, generally, (2) sewage gasification process U2

[0212] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0213] In the cooling and condensing process U203, the first sewage vaporized gas U2V-1 is separated into water-dry gas U203-V and condensed oil U203-L.

[0214] In the present invention, usually, during the heating process U204, the water-dry gas U203-V absorbs heat and heats up to become the preheated gas U203-V2;

[0215] The preheated gas U203-V2 enters the hydrogenation purification reaction process R2.

[0216] The present invention, generally, (2) sewage gasification process U2

[0217] The first sewage vaporization gas U2V-1 is a material containing dust and / or high-boiling-point phenol and / or high-boiling-point aromatic hydrocarbons;

[0218] In the oil washing liquid process KU52, the gas based on the first sewage vaporization gas U2V-1 contacts with the washing oil KU52-LF at least once to obtain the washed gas KU52-VP and washed oil KU52-LP with lower dust content and / or lower high-boiling phenol content and / or lower high-boiling aromatic hydrocarbon content, and the washed gas enters the hydrogenation purification reaction process R2;

[0219] At least a part of the wash oil KU52-LF comes from the condensed oil separated in the separation process before the washed gas KU52-VP enters the hydropurification reaction process R2, or comes from the hydrocarbon oil obtained by separating the hydropurification reaction effluent R2P.

[0220] In the present invention, (3) in the hydrogenation purification reaction process R2, two parallel-operated first branch hydrogenation purification reaction processes R2B1 and second branch hydrogenation purification reaction processes R2B2 may be provided;

[0221] When the catalyst operating conditions of the first branch hydrogenation purification reaction process R2B1 are in the final state, most to all of the materials entering the first branch hydrogenation purification reaction process R2B1 are introduced into the second branch hydrogenation purification reaction process R2B2 for hydrogenation purification reaction to extend the continuous operation period.

[0222] In the present invention, (3) in the hydrogenation purification reaction process R2, two parallel-operated first branch hydrogenation purification reaction processes R2B1 and second branch hydrogenation purification reaction processes R2B2 may be provided;

[0223] When the catalyst operating conditions of the first branch hydrogenation purification reaction process R2B1 are in the final state, all materials entering the first branch hydrogenation purification reaction process R2B1 are introduced into the second branch hydrogenation purification reaction process R2B2 for hydrogenation purification reaction, and the first branch hydrogenation purification reaction process R2B1 is isolated from the feed system of the upstream logistics U2V-1B, but hot hydrogen-rich gas is introduced for flow to maintain the operating temperature of the first branch hydrogenation purification reaction process R2B1 within a reasonable range.

[0224] In the present invention, (3) in the hydrogenation purification reaction process R2, two and / or more catalyst beds operated in series may be provided to constitute two or more sub-area hydrogenation purification reaction processes operated in series;

[0225] According to the time course, in the first stage, the logistics U2V-1B passes through the first sub-zone hydrogenation purification reaction process R201, while ensuring that at least hot hydrogen-rich gas flows through the other sub-zones to maintain the operating temperature within a reasonable range;

[0226] According to the time course, in the second stage, when the catalyst operating conditions of the first sub-area hydrogenation purification reaction process R201 are in the final state, part to all of the logistics U2V-1B entering the first hydrogenation purification reaction process R201 is introduced into the second sub-area hydrogenation purification reaction process R202 for hydrogenation purification reaction, and then it is ensured that at least hot hydrogen-rich gas flows through the first sub-area hydrogenation purification reaction process R201 to maintain the temperature of the first hydrogenation purification reaction process R201 within a reasonable range;

[0227] When the hydrogenation purification reaction process R2 is provided with 3 or more catalyst beds operated in series, according to the time course, in the third stage, when the catalyst operating conditions of the second sub-area hydrogenation purification reaction process R202 are in the final state, part to all of the logistics U2V-1B entering the second hydrogenation purification reaction process R202 is introduced into the third sub-area hydrogenation purification reaction process R203 for hydrogenation purification reaction, and then it is ensured that at least hot hydrogen-rich gas flows through the second sub-area hydrogenation purification reaction process R202 to maintain the temperature of the second hydrogenation purification reaction process R202 in a reasonable range;

[0228] By analogy, when the catalyst operating conditions of the last sub-zone hydrogenation purification reaction process R209 are in the final state, a complete operation cycle is completed, and the hydrogenation purification reaction process R2 enters the shutdown step or the first sewage low-load operation step of reducing the first sewage treatment volume.

[0229] In the present invention, usually, (3) in the hydrogenation purification reaction process R2, when the sub-area hydrogenation purification reaction process R20M processes the flow U2V-1B, the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P without passing through other sub-area hydrogenation purification reaction processes;

[0230] At the same time, the sub-area hydrogenation purification reaction processes of the other hydrogenation purification reaction processes R2, except the sub-area hydrogenation purification reaction process R20M, neither receive the logistics U2V-1B nor the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M, and only other hot water-poor hydrogen-rich gases flow through;

[0231] In the reactor of the hydrogenation purification reaction process R2, two or more or all of the sub-area hydrogenation purification reaction processes are arranged in the same pressure equipment shell and the gas phase spaces are interconnected;

[0232] All sub-areas of the hydrogenation purification reaction process R2 are arranged in one or two or more reactors.

[0233] In the present invention, usually, (3) in the first stage of the hydrogenation purification reaction process R2, when the first sub-area hydrogenation purification reaction process R201 processes the flow U2V-1B, the reaction product R201P of the first sub-area hydrogenation purification reaction process R201 is discharged from the hydrogenation purification reaction process R2 after passing through all other sub-area hydrogenation purification reaction processes located downstream, as the hydrogenation purification reaction product R2P;

[0234] When the sub-area hydrogenation purification reaction process R20M processes the flow U2V-1B, the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M passes through the downstream sub-area hydrogenation purification reaction process and is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P;

[0235] At the same time, all sub-area hydrogenation purification reaction processes located upstream of sub-area hydrogenation purification reaction process R20M do not receive logistics U2V-1B, and only other hot water-poor hydrogen-rich gases flow through, and sub-area hydrogenation purification reaction process R20M receives the effluent from the upstream sub-area hydrogenation purification reaction process;

[0236] In the reactor of the hydrogenation purification reaction process R2, two or more or all of the sub-area hydrogenation purification reaction processes are arranged in the same pressure equipment shell;

[0237] All sub-areas of the hydrogenation purification reaction process R2 are arranged in one or two or more reactors.

[0238] In the present invention, generally, the hydrocarbon feed of (3) hydrogenation reaction process R1 comprises one or more of the following fractions:

[0239] ① Hydrocarbons with a conventional boiling point of 200-350°C, including phenols and / or aromatics;

[0240] ② Hydrocarbons with a conventional boiling point of 350-450°C, including phenols and / or aromatics;

[0241] ③ Hydrocarbons with a normal boiling point of 450-550°C, including phenols and / or aromatics;

[0242] The hydrogenation reaction process R1 is a fluidized bed hydrogenation reaction process or a suspended bed hydrogenation reaction process;

[0243] The reaction effluent R1P of the hydrogenation reaction process R1 is a material containing phenols, aromatic hydrocarbons and water.

[0244] In the present invention, generally, the hydrocarbon feed of the hydrogenation reaction process R1 is a hydrocarbon stream obtained by separating the product of the direct liquefaction reaction of coal hydrogenation, and is mainly composed of hydrocarbons with a conventional boiling point of 150 to 550° C., including phenols and aromatic hydrocarbons;

[0245] The hydrogenation reaction process R1 is a fluidized bed hydrogenation reaction process and a suspended bed hydrogenation reaction process;

[0246] The reaction effluent R1P of the hydrogenation reaction process R1 is a material containing phenols, aromatic hydrocarbons and water.

[0247] In the present invention, generally, (2) the operating temperature of the first sewage vaporized gas U2V-1 obtained in the sewage gasification process U2 is at least 30° C. higher than the water dew point;

[0248] ⑶ The operating temperature of the hydrogenation purification reaction process R2 is at least 50°C higher than the water dew point, and the hydrogen partial pressure of the hydrogenation purification reaction process R2 is 6.0-18.0MPa.

[0249] In the present invention, generally, (2) the operating temperature of the first sewage vaporized gas U2V-1 obtained in the sewage gasification process U2 is at least 30° C. higher than the water dew point;

[0250] ⑶ The operating temperature of the hydrogenation purification reaction process R2 is at least 70°C higher than the water dew point, and the hydrogen partial pressure of the hydrogenation purification reaction process R2 is 9.0-14.0MPa.

[0251] In the present invention, usually, (3) in the hot high pressure separation process S1, the reaction effluent R1P of the hydrogenation reaction process R1 is separated to obtain hot high fraction gas S1-V and hot high fraction oil S1-L;

[0252] The hydrocarbon stream S1-L-TOR2 obtained by separating the hot high-fraction oil S1-L enters the hydrogenation purification reaction process R2;

[0253] The hydrocarbon stream S1-L-TOR2 is mainly composed of hydrocarbons with a conventional boiling point below 250°C and / or hydrocarbons with a boiling point of 250-320°C.

[0254] In the present invention, usually, (3) a clean hydrocarbon stream KEYS containing hydrocarbon components with a conventional boiling point of 300-350°C is subjected to a hydrogenation purification reaction process R2, and at least a portion of the clean hydrocarbon stream KEYS is maintained in a liquid phase during the hydrogenation purification reaction process R2.

[0255] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0256] Based on the cold high-pressure separation process feed of the hydrogenation purification reaction effluent R2P, it flows out of the last heat exchanger K-HX for heat recovery to become the logistics K-HX-HP, and the weight flow rate of the liquid water component in the logistics K-HX-HP is not less than 85% of the weight flow rate of the water component in the cold high-pressure water separation S7-W;

[0257] Logistics K-HX-HP, after being cooled in the cooling process, enters the cold high-pressure separation process S7.

[0258] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0259] Based on the cold high-pressure separation process feed of the hydrogenation purification reaction effluent R2P, it flows out of the last heat exchanger K-HX for heat recovery to become the logistics K-HX-HP, and the temperature of the logistics K-HX-HP is not higher than 150-170℃;

[0260] Logistics K-HX-HP, after being cooled in the cooling process, enters the cold high-pressure separation process S7.

[0261] In the present invention, (2) the washing oil U3-AL may be a heavy diesel component having a conventional boiling point of 250 to 350°C.

[0262] In the present invention, (2) the washing oil KU52-LF can be a heavy diesel component having a conventional boiling point of 250 to 350°C.

[0263] The present invention can be operated in the following manner: (1) the first sewage source

[0264] The first sewage includes sewage containing phenol, aromatic hydrocarbons and solid particles generated from the separation process of coal hydrogenation direct liquefaction reaction products, and is sewage that has undergone or has not undergone sewage pretreatment;

[0265] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0266] (2) Washing oil KU52-LF is a heavy diesel component with a conventional boiling point of 250-350°C. It is heavy diesel DIES100 distilled from the oil generated by the hydrogenation modification reaction of "coal hydrogenation direct liquefaction oil and / or hydrogenation modified oil of coal hydrogenation direct liquefaction oil", or it is the rich absorption oil formed by the heavy diesel DIES100 through the recovery of liquefied gas and gasoline containing liquefied gas and light gasoline components. In this way, heavy diesel DIES100 can be used twice in series.

[0267] The present invention can be operated in the following manner: (1) the first sewage source

[0268] The first sewage includes sewage containing phenol, aromatic hydrocarbons and solid particles generated from the separation process of coal hydrogenation direct liquefaction reaction products, and is sewage that has undergone or has not undergone sewage pretreatment;

[0269] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0270] (2) Washing oil KU52-LF is a heavy diesel component with a conventional boiling point of 250-350°C. It is heavy diesel DIES100 distilled from the oil generated by the hydrogenation modification reaction of "coal hydrogenation direct liquefaction oil and / or hydrogenation modified oil of coal hydrogenation direct liquefaction oil", or it is the rich absorption oil formed by the heavy diesel DIES100 through the recovery of liquefied gas and gasoline containing liquefied gas and light gasoline components. In this way, heavy diesel DIES100 can be used twice in series.

[0271] The present invention can be operated in the following manner: (1) the first sewage source

[0272] The first sewage, containing or not containing solid particles, is the sewage of the initial sewage with or without the sewage pretreatment process;

[0273] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0274] ⑵ Wastewater gasification process U2

[0275] In the first sewage light oil desolidification process, the first sewage is mixed with the first desolidified hydrocarbon oil feedstock and separated into the first desolidified oil-rich sewage and the first solid-reduced sewage;

[0276] The solid content in the first desolidified rich oil is higher than the solid content in the first desolidified hydrocarbon oil feedstock;

[0277] The solid content in the first solids-reducing sewage is lower than the solid content in the first sewage;

[0278] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM including water, phenol and / or aromatic hydrocarbons in the first solid reduction sewage is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0279] The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas;

[0280] The first sewage vaporized gas U2V-1 may contain or may not contain liquid hydrocarbon oil.

[0281] The present invention may be operated in the following manner: (2) in the first sewage light oil desolidification process, the first desolidified hydrocarbon oil feedstock is a hydrocarbon oil based on the condensed oil of the sewage gasification process U2, and / or is a hydrocarbon oil obtained by separating the effluent R2P of the hydrogenation purification reaction;

[0282] The first solids are removed and the oil is enriched, and then the solids are washed with oil before entering the solids removal process before the hydrogen sulfide removal and deammoniation process;

[0283] In the pre-solids removal process before the dehydrogensulfurization and deammoniation process, the first desolids-rich oil-rich logistics is mixed and contacted with the pre-wastewater logistics based on the initial wastewater to separate into pre-solids-rich oil-rich and pre-solids-reduced wastewater;

[0284] The solid content in the pre-solidification rich oil is higher than the solid content in the first desolidification rich oil;

[0285] The solid content in the front solids reduction sewage is lower than the solid content in the front sewage stream;

[0286] Based on the logistics of the pre-solid reduction sewage, it goes through the first sewage light oil desolidification process.

[0287] The present invention may be operated in such a manner that (3) the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-fraction separation process R1P-S1; the hot high-fraction oil R1P-S1L contains solid particles;

[0288] The logistics based on the hot high-fraction gas R1P-S1V is mixed and contacted with the logistics based on the first sewage to form a water-dry or water-wet first sewage vaporized gas U2V-1;

[0289] In the separation and fractionation process FRAC80, the hot high fraction oil R1P-S1L is separated into gas, narrow fraction oil products, and separation bottom oil FRAC80-DV containing solid particles;

[0290] The oil-rich logistics based on the pre-solid removal enters the separation and fractionation process FRAC80 and is mixed with the logistics based on the thermal high oil separation R1P-S1L to separate into narrow-fraction oil products. The solid particles contained in the oil-rich logistics based on the pre-solid removal enter the separation bottom oil FRAC80-DV.

[0291] The present invention may be operated in the following manner: (3) in the hydrogenation purification reaction process R2, other hydrocarbons P600 mainly composed of phenols and / or aromatics having a conventional boiling point below 350° C. are processed in combination;

[0292] Hydrocarbons P600, including or not including the hydrocarbon stream obtained by separating the oil produced by direct liquefaction of coal.

[0293] The present invention may be operated in the following manner: (3) in the hydrogenation purification reaction process R2, other hydrocarbons P700 mainly composed of phenols and / or aromatics having a conventional boiling point below 250° C. are processed jointly;

[0294] Hydrocarbons P700, including or not including the hydrocarbon stream obtained by separating the oil produced by direct liquefaction of coal.

[0295] The present invention may be operated in such a manner that (3) the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1;

[0296] The hot high-fraction oil R1P-S1L is separated and mainly contains phenol and / or aromatic hydrocarbons with a conventional boiling point below 250°C, which enter the hydrogenation purification reaction process R2 for joint processing.

[0297] The present invention can be operated in the following manner: (i) the first sewage source is sewage with low chloride ion content, selected from the top water of the distillation tower and the vacuum tower of the oil generated by direct liquefaction of coal by hydrogenation, the top water of the distillation tower of the oil generated by hydrogenation modification of direct liquefaction of coal by hydrogenation, and the acidic water of gas fractionation.

[0298] The present invention may be operated in the following manner: (3) hydrocarbon hydrogenation reaction process R1 is a hydrogenation and upgrading reaction process of coal direct liquefaction oil or coal direct liquefaction oil hydrogenation and modification oil.

[0299] The present invention can be operated in the following manner: (2) Sewage gasification process U2

[0300] The first sewage vaporized gas U2V-1 is a material containing dust and / or high-boiling-point phenols and / or high-boiling-point aromatic hydrocarbons. The gas based on the first sewage vaporized gas U2V-1 undergoes a cooling, condensation, separation and deliquescence process KU51 and / or an oil eluent process KU52 to obtain a gas with a lower dust content and / or a lower high-boiling-point phenol content and / or a lower high-boiling-point aromatic hydrocarbon content and enters the hydrogenation purification reaction process R2. DETAILED DESCRIPTION

[0301] The present invention is described in detail below.

[0302] The pressure described in the present invention is equivalent to the standard physical term pressure and refers to absolute pressure.

[0303] The conventional boiling point described in the present invention refers to the vapor-liquid equilibrium temperature of a substance at one atmospheric pressure.

[0304] The conventional boiling point range described in the present invention refers to the conventional boiling point range of the distillate.

[0305] The specific gravity described in the present invention, unless otherwise specified, refers to the ratio of the density of liquid at normal pressure and 15.6°C to the density of water at normal pressure and 15.6°C.

[0306] The composition, concentration, content or yield of the components described in the present invention are all weight-based values ​​unless otherwise specified.

[0307] The conventional gaseous hydrocarbons mentioned in the present invention refer to hydrocarbons that are gaseous under conventional conditions, including methane, ethane, propane, and butane.

[0308] The conventional liquid hydrocarbons described in the present invention refer to hydrocarbons that are liquid under conventional conditions, including pentane and hydrocarbons with higher boiling points.

[0309] The impurity elements mentioned in the present invention refer to non-hydrogen, non-carbon, non-metal components in the crude oil, such as oxygen, sulfur, nitrogen, chlorine, etc.

[0310] The impurity components mentioned in the present invention refer to the hydrogenation products of non-hydrocarbon components in the crude oil, such as water, ammonia, hydrogen sulfide, hydrogen chloride, etc.

[0311] The light hydrocarbons described in the present invention are naphtha components, which refer to conventional liquid hydrocarbons with a conventional boiling point below 200°C.

[0312] The medium hydrocarbons described in the present invention are diesel components, and refer to hydrocarbons with a conventional boiling point of 200 to 350°C.

[0313] The wax oil component described in the present invention refers to hydrocarbons with a conventional boiling point of 350 to 530°C.

[0314] The hydrogen-to-oil volume ratio mentioned in the present invention refers to the ratio of the standard volume flow rate of hydrogen to the volume flow rate of a specified oil flow at normal pressure and 20°C.

[0315] The coal direct liquefaction reaction process AR described in the present invention refers to a one-step process for producing oil products based on raw coal. It can be a coal direct liquefaction reaction process with high hydrogen consumption, such as higher than 5.0% by weight (to the coal raw material), such as a coal hydrogenation direct liquefaction reaction process, or it can be a coal direct liquefaction reaction process with low hydrogen consumption, such as lower than 2.5% by weight (to the coal raw material), such as a coal thermal solution reaction process and a coal thermal solution cracking reaction process; the coal direct liquefaction reaction process AR uses an iron-based coal direct liquefaction catalyst or a non-iron-based coal direct liquefaction catalyst, and its operating pressure can be as high as 17-25MPa or only 1.0-2.5MPa; the reaction process R100, its operating temperature can usually reach 400-465°C.

[0316] In the coal direct liquefaction reaction process AR of the present invention, no matter how much the chemical hydrogen consumption in the reaction process is, the distillation oil of conventional liquid hydrocarbons obtained by separating the oil generated by the coal direct liquefaction reaction is called coal direct liquefaction oil, which is a hydrocarbon oil with a high aromatic carbon rate (usually higher than 0.40, generally higher than 0.66, and even higher than 0.8), that is, a high aromatic oil. Due to the wide distribution of carbon numbers of hydrocarbon products of the coal direct liquefaction reaction, according to the selected distillation range of the coal direct liquefaction oil, the coal direct liquefaction oil can be a conventional boiling range below 560°C, that is, containing conventional aromatic hydrocarbons. The conventional boiling range of 500-560°C for 6-ring aromatic hydrocarbons, the coal direct liquefaction oil can be 50-500°C, that is, it basically does not contain 6-ring aromatic hydrocarbons with a conventional boiling point of 500-560°C; of course, the coal direct liquefaction oil can also contain light residual oil components with a conventional boiling range higher than 560°C, that is, it contains polycyclic aromatic hydrocarbons with more than 7 rings with a conventional boiling point of 560-650°C; the coal direct liquefaction oil, whose conventional boiling range is higher than 650°C, usually belongs to the heavy residual oil component, which usually constitutes the distillation bottom oil in the unevaporated oil in the distillation process.

[0317] Since coal powder participates in the reaction in the form of oil-coal slurry, the basic conditions for coal direct liquefaction reaction, such as coal powder dispersion, hydrocarbon molecule diffusion, hydrogen molecule dissolution, and catalyst dispersion, can be achieved. Therefore, the coal direct liquefaction reaction process AR is also called the oil-coal slurry direct liquefaction reaction process R100.

[0318] The coal direct liquefaction reaction process AR described in the present invention refers to a reaction process in which coal and possibly existing molecular hydrogen are used as raw materials, a specific oil product (usually coal direct liquefaction oil or hydrogenated modified oil of coal direct liquefaction oil) is used as solvent oil, and under certain operating conditions (such as operating temperature, operating pressure, solvent oil / coal weight ratio, hydrogen / solvent oil volume ratio and suitable hydrogenation catalyst), the coal directly undergoes carbon-carbon bond thermal cracking, free radical hydrogenation modification, hydrocarbon oil hydrorefining, hydrocarbon oil hydrocracking and other hydrogenation liquefaction reactions.

[0319] The coal direct liquefaction oil described in the present invention refers to the distillate oil obtained by separating the oil generated by the direct liquefaction reaction of coal by hydrogenation. It exists in the effluent of the direct liquefaction reaction of coal by hydrogenation, and is a comprehensive reaction product based on solvent oil, coal consumed in the reaction, and hydrogen transferred by the reaction. It can be a mixed oil of at least any two of the conventional boiling point fraction segment <195°C, the 195°C to 280°C fraction segment, the 280°C to 560°C fraction segment, and the 560°C to 650°C fraction segment. It can be any fraction segment within the range of 195°C to 650°C, and is usually any fraction segment within the range of 195°C to 560°C.

[0320] Depending on the source of the raw coal and the different coal direct liquefaction reaction conditions, the hydrogen content, aromatic carbon rate, organic nitrogen content, organic oxygen content and >350°C fraction yield of coal direct liquefaction oil from different sources are different and fluctuate within a large range. Usually, the hydrogen content is 5.0-11.2wt%, the aromatic carbon rate is 0.23-0.98mol%, the organic nitrogen content is 0.20-1.5wt%, the organic oxygen content is 0.40-6.30wt%, the >350°C fraction yield is 15-65wt%, and the >500°C fraction yield is 5-25wt%.

[0321] The hydrogenation and modification reaction process BR of coal direct liquefaction oil described in this article refers to the hydrogenation reaction process of converting coal direct liquefaction oil into hydrocarbons with lower aromatic carbon rate and lower impurity content, such as producing hydrogenation and upgrading raw oil, hydrogenation and modification oil with specific impurity content, hydrogenation and modification oil with specific aromatic carbon rate content, hydrogenation and modification oil of specific boiling range distillate oil, etc. The oil generated by the fractionation and hydrogenation modification reaction is obtained to obtain oil products of different boiling range distillation segments, and then blended to obtain oil products for different purposes, such as hydrogenation and modification solvent oil entering the coal direct liquefaction reaction process AR. The hydrogenation and modification solvent oil has a hydrogenation index PDQI index usually greater than 22 mg / g, generally greater than 24 mg / g. The hydrogenation and modification solvent oil is usually used as coal slurry solvent oil, flushing oil of the plunger rod stuffing box of the plunger raw coal slurry pump, high-pressure instrument flushing oil, pipeline flushing oil and passes through at least a part of the reaction space of the coal hydrogenation and direct liquefaction reaction process R100.

[0322] The hydrogenation upgrading reaction process CR of coal direct liquefaction oil described in this article refers to using coal direct liquefaction oil and / or narrow-fraction oil of coal direct liquefaction oil hydrogenation modification reaction product oil as raw material, at least performing deep hydrogenation refining reaction, and possibly performing selective hydrogenation ring-opening reaction, and even performing hydrocracking reaction, and the quality indicators of the produced hydrogenation modification product oil are determined according to needs, usually the weight content of organic nitrogen is less than 3-10ppm, the weight content of organic sulfur is less than 5-20ppm, and the aromatics content is determined according to needs.

[0323] The aromatic carbon ratio of hydrocarbons refers to the ratio of the number of aromatic carbon atoms to the total number of carbon atoms in the hydrocarbon molecule.

[0324] The hydrogen supply index PDQI of hydrocarbons refers to the number of milligrams of active hydrogen at the β position of the cycloalkyl group in cycloalkyl aromatic hydrocarbons per gram of hydrocarbons.

[0325] For coal direct liquefaction oil or coal direct liquefaction oil hydrogenation modification reaction product oil, which are aromatic-rich mixtures composed of various hydrocarbons with different boiling points, there is a macroscopic correspondence between the hydrogen supply index PDQI of hydrocarbons and their aromatic carbon ratio.

[0326] The gas holdup rate of the logistics in the hydroprocessing reactor refers to the volume ratio of the gas phase in the logistics.

[0327] The liquid holdup of the logistics in the hydroprocessing reactor refers to the volume ratio of the liquid phase in the logistics.

[0328] The hydrogen-to-oil ratio of the present invention may be the ratio of the standard volume flow rate of the hydrogen-rich gas stream to the weight of the feedstock oil, and the unit is standard cubic meter / ton, i.e. Nm 3 / t.

[0329] The feed hydrogen / feed oil volume ratio of the hydroprocessing reactor of the present invention refers to the ratio of the standard state volume flow rate of the hydrogen-rich gas flow to the standard state volume of the feed oil, and the unit is standard cubic meter / cubic meter, i.e. Nm 3 / m 3 .

[0330] The hydrogen / oil volume ratio at a certain point in the hydrogenation reactor of the present invention refers to the ratio of the standard state volume flow rate of the gas phase to the standard state volume of the liquid material, and the unit is standard cubic meter / cubic meter, that is, Nm 3 / m 3 .

[0331] The catalyst liquid hourly space velocity in the hydroprocessing reactor of the present invention refers to the ratio of the volume flow rate of the processed fresh crude oil at 0.1 MPaA and 20°C to the static accumulation state volume of the hydroprocessing catalyst, and the unit is h -1 .

[0332] A common coal direct liquefaction reaction process AR may be a coal hydrogenation direct liquefaction reaction process R100.

[0333] The hydrogenation modification reaction process BR of coal direct liquefaction oil can be the hydrogenation modification reaction process of the production of hydrogen-donating solvent oil for producing high aromatic oil by coal hydrogenation direct liquefaction, also known as the solvent oil hydrogenation modification reaction process.

[0334] For coal direct liquefaction oil with shallow hydrogenation depth and low chemical hydrogen consumption, the coal direct liquefaction oil has stronger polarity and greater viscosity, so it carries more solid particles. It must adopt the boiling bed hydrogenation modification reaction method. At the same time, its aromatic carbon rate is higher and the heteroatom content is higher. When the hydrogenation modification oil with low aromatic carbon rate is generated through the hydrogenation modification reaction process BR, the chemical hydrogen consumption is higher and the amount of heteroatom hydrogenation products is higher. Its operation method is completely different from the conventional high-hydrogen consumption coal hydrogenation direct liquefaction to produce high aromatic oil with low hydrogen consumption and low impurity hydride production hydrogenation modification reaction process BR, which requires multi-stage or multi-stage hydrogenation modification reaction process BR.

[0335] The hydrogen-donating hydrocarbons described in the present invention refer to partially saturated bicyclic aromatic hydrocarbons and partially saturated polycyclic aromatic hydrocarbons, which are hydrocarbon components with hydrogen-donating function in the direct oil production reaction process of coal hydrogenation. The hydrogen-donating hydrocarbons include partially saturated bicyclic aromatic hydrocarbons and partially saturated polycyclic aromatic hydrocarbons, which are ideal components of hydrogen-donating solvent oil used in the direct liquefaction process of coal hydrogenation. Among the hydrogen-donating hydrocarbons, the hydrogen-donating speed of the dihydrogenated hydrocarbons is greater than that of the tetrahydrogenated hydrocarbons. The hydrogen-donating speed of the dihydrogenated hydrocarbons of tricyclic aromatic hydrocarbons is higher or lower than that of the dihydrogenated hydrocarbons of bicyclic aromatic hydrocarbons. Experiments have shown that although polycyclic aromatic hydrocarbons have no hydrogen-donating ability, they have the ability to transfer hydrogen.

[0336] The hydrogen-donating solvent oil described herein refers to a hydrocarbon oil rich in hydrogen-donating hydrocarbons that has the ability to donate hydrogen in the R100 direct liquefaction reaction process of coal hydrogenation.

[0337] The coal hydrogenation direct liquefaction reaction process R100 of the present invention refers to a method for directly liquefying coal by hydrogenation in the presence of solvent oil. There are many different processes according to different solvent oils, catalysts and hydrogenation process conditions, such as the following processes:

[0338] ①Solvent hydrogenation extraction liquefaction method: such as solvent refined coal method I and II (SRC-I and SRC-II), hydrogen supply solvent oil method EDS, Japan New Energy Development Organization liquefaction method (NEDOL), etc., using hydrogen, but the pressure is not too high, solvent oil has a significant effect;

[0339] ② High-pressure catalytic hydrogenation method: such as Germany's new and old liquefaction processes (IG and NewIG) and the United States' hydrogen coal method (H-Coal) belong to this category;

[0340] ③ Co-processing of coal and residual oil: residual oil is used as solvent oil and passes through the reactor together with coal at one time without circulating oil; the residual oil is hydrocracking to convert into light oil at the same time. The United States, Canada, Germany and the Soviet Union have different processes;

[0341] ④ China Shenhua Group's coal direct liquefaction method;

[0342] ⑤ Patent CN100547055C states a hot-melt catalytic method for producing liquid fuel from lignite, which belongs to the process of direct liquefaction of lignite by medium-pressure hydrogenation, including two processes: coal hydrogenation direct liquefaction reaction process R100 and coal direct liquefaction oil hydrogenation modification process. In order to improve the conversion rate of coal direct liquefaction and realize the entry of coal raw materials into the coal hydrogenation direct liquefaction reactor, coal is usually made into coal powder before entering the coal hydrogenation direct liquefaction reactor, and is mixed with solvent oil with good hydrogen supply capacity to form oil-coal slurry, which enters the coal hydrogenation direct liquefaction reactor after pressurization and heating.

[0343] In the process of direct liquefaction of coal by hydrogenation, no matter what kind of direct liquefaction process of coal by hydrogenation, the goal is to obtain oil products, the function pursued is "coal to oil", and the chemical change that must exist is "coal hydrogenation". The common characteristics of this type of technology at present are the use of solvent oil and catalyst. The conventional boiling range of solvent oil is generally 195-530°C, and most of them are 195-450°C. Most of the solvent oil is distilled oil or its hydrogenated modified oil. Most of the aromatic hydrocarbons contained are aromatic hydrocarbons with 2-4 ring structures, and contain a small amount of 5-ring structure aromatic hydrocarbons. Therefore, no matter what kind of direct liquefaction process of coal by hydrogenation, the effluent oil or coal direct liquefaction oil (usually coal hydrogenation direct liquefaction light oil) or coal direct liquefaction oil stabilized oil produced by it, as long as its composition has the raw material composition characteristics described in the present invention, can be processed using the method of the present invention.

[0344] The coal hydrogenation direct liquefaction reaction process R100, macroscopically speaking, is both a hydrogenation direct liquefaction reaction process of coal carried by coal slurry, a hydrogenation process (or dehydrogenation process) of the hydrogen-donating solvent oil carried by the coal slurry, and a hydrocracking reaction process in which the carbon number of hydrocarbon components (such as hydrocarbons with a conventional boiling point higher than 290°C) in the net oil produced by coal hydrogenation direct liquefaction is reduced.

[0345] The coal direct liquefaction oil refers to the distilled oil obtained by separating the oil generated by the coal hydrogenation direct liquefaction reaction. It exists in the effluent of the coal hydrogenation direct liquefaction reaction. It is a comprehensive reaction product based on the hydrogen supply solvent oil, the coal consumed in the reaction and the hydrogen transferred by the reaction. It is classified according to the maximum number of aromatic ring structures. It includes a conventional boiling point <195°C fraction segment (the maximum number of aromatic ring aromatics is monocyclic aromatics), a 195°C~280°C fraction segment (the maximum number of aromatic ring aromatics is dicyclic aromatics), and a 280°C~540°C fraction segment (the maximum number of aromatic ring aromatics is polycyclic aromatics). It can be a mixture of 1, 2 or more oils with different properties.

[0346] The conventional boiling point <195℃ fraction of coal direct liquefaction oil or its hydrogenation and modification reaction product oil is usually not used as a candidate coal slurry solvent oil or hydrogen supply solvent oil for the coal hydrogenation and direct liquefaction reaction process R100, because the proportion of R100 modified fraction oil evaporating into the gas phase in the coal hydrogenation and direct liquefaction reaction process is too high. The conventional boiling point <195℃ fraction of coal direct liquefaction oil basically does not contain aromatic rings with two ring structures such as tetralin, dilin, and naphthalene, so it does not have the raw material aromatic ring structure for hydrogenation and modification to generate hydrogen supply hydrocarbons.

[0347] The normal boiling point of coal direct liquefaction oil is in the 280℃~540℃ fraction range, and the aromatic hydrocarbons it contains are mainly polycyclic aromatic hydrocarbons.

[0348] The normal boiling point of coal direct liquefaction oil is 280℃~370℃ fraction, containing tricyclic aromatic hydrocarbons.

[0349] The normal boiling point of coal direct liquefaction oil is 370℃~470℃ fraction, containing tetracyclic aromatic hydrocarbons.

[0350] The normal boiling point of coal direct liquefaction oil is 470℃~525℃ fraction, containing pentacyclic aromatic hydrocarbons.

[0351] The normal boiling point of coal direct liquefaction oil is 525℃~550℃ fraction, containing six-ring aromatic hydrocarbons.

[0352] Usually, coal direct liquefaction oil contains a certain amount of aromatic hydrocarbons with more than five rings and gums, which exist in the fractions with conventional boiling points > 470°C. In order to prevent the deterioration of the properties of the BR raw oil in the hydrogenation modification reaction process, their content is generally controlled at a lower value, usually 4 to 9 weight % of the total raw oil. The presence of these substances will accelerate the coking rate of the hydrogenation modification catalyst in the hydrogenation modification reaction process BR.

[0353] After the coal hydrogenation direct liquefaction reaction process R100 operates normally, the hydrogen supply solvent oil is usually the hydrogenated modified oil of the coal direct liquefaction oil (usually the distillate oil with the conventional boiling range higher than 200°C) produced by the coal hydrogenation direct liquefaction reaction process R100. The main goal of the coal direct liquefaction oil hydrogenation modification reaction process BR is to produce the slurry solvent oil for the coal slurry of the coal hydrogenation direct liquefaction reaction raw material. Specifically, it is to increase the content of "components with good hydrogen supply function" in the oil product, such as increasing the content of cycloalkylbenzene and dicycloalkylbenzene components. Based on the fact that the coal direct liquefaction oil contains a large amount of dicyclic aromatic hydrocarbons and a large amount of polycyclic aromatic hydrocarbons, the coal direct liquefaction oil hydrogenation modification reaction process BR is a "moderate aromatic hydrogenation saturation reaction process" of dicyclic aromatic hydrocarbons and polycyclic aromatic hydrocarbons.

[0354] The ultimate goal of the coal hydrogenation direct liquefaction reaction process R100 is to produce oil products for external supply. Usually, the hydrogenated modified oil produced by the coal direct liquefaction oil hydrogenation modification reaction process BR is divided into two parts: one part is used as the hydrogen supply solvent oil for the coal hydrogenation direct liquefaction reaction process R100, and the other part is used as the external discharge oil of the coal hydrogenation direct liquefaction oil production process. Usually, at least a part of the coal hydrogenation direct liquefaction light oil produced by the coal hydrogenation direct liquefaction reaction process R100 is used as the external discharge oil A of the coal-to-oil process, and the rest of the coal direct liquefaction oil is used as the raw oil of the coal hydrogenation modification reaction process BR to produce the hydrogen supply solvent oil and external discharge oil B for the coal hydrogenation direct liquefaction reaction process R100. At this time, there are two external discharge oils, A and B. The final destination of the two external discharge oils A and B is usually to produce high-quality oil products such as diesel fraction and naphtha fraction through the hydrogenation quality improvement reaction process CR.

[0355] The following describes the general control principle of the gas phase hydrogen sulfide concentration in the hydrogenation reaction process of the present invention.

[0356] For the heavy oil suspension bed hydrocracking process with high nitrogen content and low sulfur content, in order to maintain the minimum hydrogen sulfide partial pressure of the initial reaction process, any kind of supplementary sulfur can be added to any hydrogenation reaction process as needed, but it is usually added to the inlet of the most upstream hydrogenation reaction process to ensure the minimum hydrogen sulfide concentration required for the reaction process, such as 500ppm (v) or 1000ppm (v) or 3000ppm (v) and other expected specified values, to ensure that the hydrogen sulfide partial pressure required by the catalyst is not lower than the minimum specified value, to ensure the required sulfidation form of the catalyst. The supplementary sulfur can be a material containing hydrogen sulfide or that can be converted into hydrogen sulfide and has no adverse effect on the hydroconversion process, such as gas or oil containing hydrogen sulfide, or liquid sulfur or carbon disulfide or dimethyl disulfide that generates hydrogen sulfide after contacting with high-temperature hydrogen.

[0357] The general principles of the high pressure separation process of the hydrogenation reaction effluent of the present invention are described in detail below.

[0358] The high-pressure separation process of the hydrogenation reaction effluent usually includes a cold high-pressure separator. When the hydrocarbon oil in the hydrogenation reaction effluent has a high density (for example, close to the density of water) or a high viscosity or is difficult to separate from water or contains solid particles, it is also necessary to set a hot high-pressure separator with an operating temperature of usually 150-450°C. At this time, the hydrogenation reaction effluent enters the hot high-pressure separator and is separated into a hot high-fraction gas mainly composed of hydrogen and a hot high-fraction oil liquid mainly composed of conventional liquid hydrocarbons and possible solids. The hot high-fraction gas enters the cold high-pressure separator with an operating temperature of usually 20-80°C and is separated into cold high-fraction oil and cold high-fraction gas. Since a large number of high-boiling point components enter the hot high-fraction oil liquid, the following goals are achieved: the cold high-fraction oil density becomes smaller or the viscosity becomes smaller or it is easy to separate from water. The high-pressure separation process of the hydrogenation reaction effluent is equipped with a hot high-pressure separator, which also has the advantage of reducing heat loss, because the hot high-fraction oil liquid can avoid the cooling process of the hot high-fraction gas using an air cooler or a water cooler. At the same time, part of the hot high-fraction oil liquid can be returned to the upstream hydrogenation reaction process for recycling to improve the overall feed properties of the hydrogenation reaction process receiving the circulating oil, or to perform cyclic hydrogenation on the circulating hot high-fraction oil.

[0359] A warm and high-pressure separation part can be set between the hot high-pressure separation part and the cold high-pressure separation part as needed. At this time, the hot high-fraction gas becomes a gas-liquid two-phase material after cooling, and is separated in the warm and high-pressure separator into a warm high-fraction gas mainly composed of hydrogen and a warm high-fraction oil liquid mainly composed of conventional liquid hydrocarbons and possible solids. The warm high-fraction gas enters the cold high-pressure separation part for cooling and gas-liquid separation.

[0360] Before the hydrogenation reaction effluent or hot high fraction gas or warm high fraction gas enters the cold high pressure separation process, the temperature is usually lowered (usually there is heat exchange with the reaction process feed) to about 220-100°C (the temperature should be higher than the crystallization temperature of ammonium hydrosulfide and ammonium chloride in the gas phase of the hydrogenation reaction effluent), and then washing water is usually injected into it to form the water-injected hydrogenation reaction effluent. It may be necessary to set up 2 or more water injection points. The washing water is used to absorb ammonia and other impurities that may exist, such as hydrogen chloride, hydrogen sulfide, etc., and the aqueous solution after absorbing ammonia must absorb hydrogen chloride and hydrogen sulfide. In the cold high pressure separation process, the water-injected hydrogenation reaction effluent is separated into: a cold high fraction gas mainly composed of hydrogen in volume, a cold high fraction oil mainly composed of conventional liquid hydrocarbons and dissolved hydrogen, and a cold high fraction water mainly composed of water and dissolved ammonia and hydrogen sulfide. The ammonia content of the cold high fraction water is generally 0.5-15% (w), preferably 1-8% (w). One purpose of injecting washing water is to absorb ammonia and hydrogen sulfide in the hydrogenation reaction effluent, to prevent the formation of ammonia hydrogen sulfide or polysulfur ammonia crystals to block the heat exchanger channel and increase the system pressure drop. The injection amount of the washing water should be determined according to the following principles: on the one hand, the washing water is divided into vapor phase water and liquid phase water after being injected into the hydrogenation reaction effluent, and the amount of liquid phase water must be greater than zero, preferably 30% or more of the total amount of washing water; on the other hand, the washing water is used to absorb ammonia in the hydrogenation reaction effluent to prevent the ammonia concentration of the high fraction gas from being too high and reducing the catalyst activity. Generally, the lower the ammonia volume concentration of the high fraction gas, the better, generally not more than 200ppm (v), preferably not more than 50ppm (v). The operating pressure of the cold high-pressure separator is the pressure of the hydrogenation reaction process minus the actual pressure drop. The difference between the operating pressure of the cold high-pressure separation process and the hydrogenation reaction pressure should not be too low or too high, generally 0.35~3.2MPa, usually 0.5~1.5MPa. The hydrogen volume concentration of the cold high-fraction gas should not be too low (resulting in an increase in the operating pressure of the device), and should generally be no less than 70% (v), preferably no less than 80% (v), and preferably no less than 85% (v). As mentioned above, at least one process, usually 85-100% of the cold high-fraction gas is returned to the hydrogenation reaction process for recycling to provide the necessary hydrogen amount and hydrogen concentration for the hydrogenation reaction process; in order to improve the investment efficiency of the device, it is necessary to ensure that the circulating hydrogen concentration is not lower than the aforementioned lower limit. To this end, according to the specific raw material properties, reaction conditions, and product distribution, a portion of the cold high-fraction gas can be removed to remove the methane and ethane produced by the reaction. For the discharged cold high-fraction gas, conventional membrane separation processes, pressure swing adsorption processes, or oil washing processes can be used to separate hydrogen and non-hydrogen gas components, and the recovered hydrogen can be used as new hydrogen.

[0361] For the hydrocarbon material upflow expanded bed staged hydrogenation reaction process of the present invention, when the conventional non-hydrogen gas product yield is large, usually part or all of the cold high-fraction gas, such as about 30 to 100% of the cold high-fraction gas, is purified by a membrane separation process, and the resulting permeated hydrogen is pressurized and returned to the hydrogenation reaction process, and the non-permeated gas is discharged to control the volume concentration of the non-hydrogen components in the circulating gas; after the non-permeated gas is discharged, it can be subjected to PSA hydrogen extraction or "steam reforming hydrogen production + PSA hydrogen extraction" to obtain high-purity hydrogen, which is pressurized and returned to the hydrogenation reaction process for recycling.

[0362] New hydrogen enters the hydrogenation part to supplement the hydrogen consumed in the hydrogenation reaction process. The higher the hydrogen concentration of the new hydrogen, the better. Generally, it should not be lower than 95% (v), and preferably not lower than 99% (v). All the new hydrogen can be introduced into any hydrogenation reaction part, preferably into the first hydrogenation reactor.

[0363] In the present invention, in any reaction process, the hydrogen gas stream used may be all new hydrogen, all recycled hydrogen, or a mixture of new hydrogen and recycled hydrogen.

[0364] In the feeding process of the hydrogenation purification reaction process R2 of the present invention, in order to remove dust, phenols that are difficult to hydrogenate and aromatic hydrocarbons and other polluting components so that they do not pass through the hydrogenation purification reaction process R2, the feed containing dust, macromolecular phenols and macromolecular aromatic hydrocarbons of the hydrogenation purification reaction process R2 undergoes a cooling, condensing, separating and deliquating process or an oil washing liquid process, and then the obtained gas phase is heated and then enters the hydrogenation purification reaction process R2; the washing oil of the feed gas phase of the hydrogenation purification reaction process R2 comes from the condensed oil separated in the separation process after the feed gas phase of the hydrogenation purification reaction process R2 is washed but before entering the hydrogenation purification reaction process R2, or from the hydrocarbon oil obtained by separating the hydrogenation purification reaction effluent R2P; the above-mentioned oil washing process also has the effect of reducing the boiling range dry point and density of the total hydrocarbons in the reaction product of the hydrogenation purification reaction process R2, which is beneficial to reducing the equilibrium solubility of hydrocarbons in cold high-fraction water, and reducing the dissolved hydrocarbons in cold high-fraction water has the effect of reducing the boiling range dry point and density.

[0365] From another perspective, the goal of the hydrogenation purification reaction process R2 of the present invention is to ensure the clean operation of the hydrogenation purification reaction effluent R2P, which is why it is called the hydrogenation purification reaction process R2.

[0366] The characteristic parts of the present invention are described below.

[0367] The present invention provides a method for hydrogenating and purifying evaporated gas of wastewater containing phenol and / or aromatic hydrocarbons, which is characterized by comprising the following steps:

[0368] The pollutant components KC contained in the first sewage include phenol and / or aromatic hydrocarbons, include or exclude solid particles, and include or exclude other pollutant components that can undergo hydrogenation conversion reactions in the hydrogenation purification reaction process R2 to reduce their molecular electrical conductivity;

[0369] The heteroatom-containing organic matter includes oxygen-containing organic matter, includes or excludes nitrogen-containing organic matter, includes or excludes sulfur-containing organic matter, includes or excludes chlorine-containing organic matter;

[0370] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0371] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to produce organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to produce aromatic hydrocarbons with a lower aromatic carbon rate.

[0372] The present invention is usually operated as follows:

[0373] ⑴The first source of sewage

[0374] The first sewage, containing or not containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0375] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0376] ⑵ Wastewater gasification process U2

[0377] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0378] The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas;

[0379] The first sewage vaporized gas U2V-1 contains or does not contain liquid hydrocarbon oil;

[0380] ⑶ Hydrogenation purification reaction process R2

[0381] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0382] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0383] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0384] The present invention generally operates in the following manner:

[0385] ⑴The first source of sewage

[0386] The source of the first wastewater includes one or more of the following processes: coal hydrogenation direct liquefaction process, coal gasification process, coal dry distillation process, coal tar processing process;

[0387] The first sewage, containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0388] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal;

[0389] ⑵ Wastewater gasification process U2

[0390] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0391] The first sewage vaporization gas U2V-1 is water dry gas;

[0392] The first sewage vaporized gas U2V-1 contains liquid hydrocarbon oil;

[0393] ⑶ Hydrogenation purification reaction process R2

[0394] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the water-dry stream U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0395] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0396] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0397] The present invention generally operates as follows:

[0398] ⑴The first source of sewage

[0399] The first sewage, containing or not containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0400] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal;

[0401] ⑵ Wastewater gasification process U2

[0402] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0403] The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas;

[0404] The first sewage vaporized gas U2V-1 contains or does not contain liquid hydrocarbon oil;

[0405] ⑶ Hydrocarbon hydrogenation reaction process R1 and hydrogenation purification reaction process R2

[0406] A hydrogen-containing gas phase stream R1P-VB based on the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is subjected to a hydrogenation purification reaction process R2;

[0407] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0408] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0409] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics R1P-VB undergoes a hydrogenation refining purification reaction of at least a portion of the pollutant components to be converted into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0410] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics R1P-VB undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0411] In the hydrogenation purification reaction process R2, the components based on the stream U2V-1B or the intermediate hydrogenation products based on the components of the stream U2V-1B are mixed and contacted with the stream R1P-VB or the intermediate hydrogenation products of the stream R1P-VB;

[0412] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0413] The present invention generally operates as follows:

[0414] ⑴The first source of sewage

[0415] The source of the first wastewater includes one or more of the following processes: coal hydrogenation direct liquefaction process, coal gasification process, coal dry distillation process, coal tar processing process;

[0416] The first sewage, containing solid particles, is sewage that has or has not undergone a sewage pretreatment process;

[0417] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal;

[0418] ⑵ Wastewater gasification process U2

[0419] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0420] The first sewage vaporization gas U2V-1 is water dry gas;

[0421] The first sewage vaporized gas U2V-1 contains liquid hydrocarbon oil;

[0422] ⑶ Hydrocarbon hydrogenation reaction process R1 and hydrogenation purification reaction process R2

[0423] A hydrogen-containing gas phase stream R1P-VB based on the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is subjected to a hydrogenation purification reaction process R2;

[0424] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0425] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0426] In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics R1P-VB undergoes a hydrogenation refining purification reaction of at least a portion of the pollutant components to be converted into a hydrogenation purification reaction effluent R2P with a low organic pollutant content;

[0427] In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics R1P-VB undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate;

[0428] In the hydrogenation purification reaction process R2, the components based on the stream U2V-1B or the intermediate hydrogenation products based on the components of the stream U2V-1B are mixed and contacted with the stream R1P-VB or the intermediate hydrogenation products of the stream R1P-VB;

[0429] The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

[0430] In the present invention, usually, the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is a stream containing phenol, aromatic hydrocarbons, water and hydrogen.

[0431] In the present invention, generally, the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1;

[0432] The logistics based on the hot high-fraction gas R1P-S1V is mixed and contacted with the logistics based on the first sewage to form water-dry or water-wet first sewage vaporized gas U2V-1.

[0433] The present invention, generally, (3) sets a sewage spray gasification process WDV;

[0434] In the sewage spray gasification process WDV, a liquid water-containing logistics based on the first sewage is sprayed into a gas-containing logistics based on the hot high-fraction gas R1P-S1V for vaporization to form a logistics containing water-dry first sewage vaporized gas U2-2. The operating temperature of the water-dry first sewage vaporized gas U2-2 is lower than the operating temperature of the logistics R1P-S1V, with or without the generation of condensed oil WDV-L.

[0435] In the present invention, generally, (3) during the sewage spray gasification process WDV, condensed oil WDV-L is produced;

[0436] Condensate oil WDV-L, with or without solid particles from the first sewage.

[0437] In the present invention, usually, (3) in the wastewater spray gasification process WDV, the condensed oil WDV-L is separated so that it does not undergo the hydrogenation purification reaction process R2.

[0438] In the present invention, usually, (3) in the cold high-pressure separation process S7, the water-containing and hydrogen-containing flow based on the hydrogenation purification reaction effluent R2P is separated to obtain cold high-pressure water separation S7-W.

[0439] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0440] At least a portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrogenation purification reaction effluent R2P for recycling.

[0441] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0442] At least a portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrocarbon hydrogenation reaction process R1 for recycling.

[0443] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0444] A portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrocarbon hydrogenation reaction process R1 for recycling;

[0445] A portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrogenation purification reaction effluent R2P for recycling without passing through the hydrocarbon hydrogenation reaction process R1.

[0446] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0447] The hydrogen concentration in the cold high-fraction gas S7-V is 75 to 98 volume %.

[0448] In the present invention, generally, the reaction index of (3) hydrogenation purification reaction process R2 is as follows:

[0449] The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 80%;

[0450] The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 80%;

[0451] The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 80%;

[0452] In the hydrogenation purification reaction process R2, the hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon reduces the aromatic carbon ratio by more than 60%;

[0453] The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 70%;

[0454] The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%;

[0455] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 35 weight %;

[0456] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 15 weight %;

[0457] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 10 weight %.

[0458] In the present invention, generally, the reaction index of (3) hydrogenation purification reaction process R2 is as follows:

[0459] The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 90%;

[0460] The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 90%;

[0461] The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 90%;

[0462] In the hydrogenation purification reaction process R2, the hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon reduces the aromatic carbon ratio by more than 70%;

[0463] The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%;

[0464] The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 90%;

[0465] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 17.5 weight %;

[0466] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 7.5 weight %;

[0467] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 5.0 weight %.

[0468] The present invention preferably has the following reaction indexes in the (3) hydrogenation purification reaction process R2:

[0469] The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 98%;

[0470] The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 98%;

[0471] The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 98%;

[0472] The hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%;

[0473] The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 90%;

[0474] The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 95%;

[0475] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 9 weight %;

[0476] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 6 weight %;

[0477] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 3 weight %.

[0478] In the present invention, generally, the purification index of (3) hydrogenation purification reaction process R2 is as follows:

[0479] The weight content of organic oxygen in the hydrocarbons in the hydropurification reaction effluent R2P is less than 5 ppm;

[0480] The weight content of organic nitrogen in the hydrocarbons in the hydropurification reaction effluent R2P is less than 5 ppm;

[0481] The organic sulfur content in the hydrocarbons in the hydropurification reaction effluent R2P is less than 2 ppm by weight.

[0482] In the present invention, generally, the purification index of (3) hydrogenation purification reaction process R2 is as follows:

[0483] The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 5 weight %;

[0484] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 2 weight %;

[0485] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 1 weight %.

[0486] In the present invention, generally, the operating conditions of the hydrogenation purification reaction process R2 are: pressure of 6 to 25 MPa, temperature of 220 to 440°C, hydrogen to oil ratio of 2000 to 20000 Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.05~10.0h -1 .

[0487] In the present invention, generally, the operating conditions of the hydrogenation purification reaction process R2 are: pressure of 12-20 MPa, temperature of 270-390°C, hydrogen-to-oil ratio of 2000-20000 Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.2~1.0h -1 .

[0488] In the present invention, generally, the raw hydrocarbons in the hydrocarbon hydrogenation reaction process R1 are hydrocarbon materials containing phenols and aromatics, including hydrocarbons with a conventional boiling point higher than 350°C;

[0489] The operating conditions of hydrocarbon hydrogenation process R1 are usually: pressure of 6-25 MPa, temperature of 220-460°C, hydrogen-to-oil ratio of 100-3000 Nm 3 / t;

[0490] The operating conditions of the hydrogenation purification reaction process R2 are usually: pressure of 6-25MPa, temperature of 220-440℃, hydrogen-to-oil ratio of 2000-20000Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.05~10.0h -1 .

[0491] In the present invention, generally, the raw hydrocarbons of the hydrocarbon hydrogenation reaction process R1 are hydrocarbon materials containing phenols and aromatics, including hydrocarbons with a conventional boiling point higher than 350°C;

[0492] The operating conditions of hydrocarbon hydrogenation process R1 are generally: pressure of 12-20 MPa, temperature of 320-440°C, hydrogen-to-oil ratio of 200-2000 Nm 3 / t;

[0493] ⑶ The operating conditions of hydrogenation purification reaction process R2 are generally: pressure of 12-20MPa, temperature of 270-390℃, hydrogen-to-oil ratio of 2000-20000Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.2~1.0h -1 .

[0494] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0495] Cold high-purity water S7-W has a phenol content of less than 10ppm and an aromatic content of less than 200ppm.

[0496] In the present invention, generally, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high fraction gas S7-V, cold high fraction water S7-W, and cold high fraction oil S7-L;

[0497] Cold high-purity water S7-W has a phenol content of less than 5ppm and an aromatic content of less than 50ppm.

[0498] In the present invention, generally, (2) in the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM containing water, phenol and / or aromatic hydrocarbons in the first sewage is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0499] In the first oil washing process U3, the logistics U2V-1VB based on the first sewage vaporized gas U2V-1 contacts the washing oil U3-AL at least once to obtain the first washed gas U3-PV and the first washed oil U3-PL;

[0500] The amount of solids in the first washed gas U3-V is less than the amount of solids in the gas phase of the stream U2V-1VB.

[0501] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0502] At least a part of the stream based on the cold high fraction oil S7-L is recycled as wash oil U3-AL.

[0503] In the present invention, generally, (3) a gas-phase-containing stream R2P-VB based on the hydrogenation purification reaction effluent R2P is mixed with a quenching stream KS and cooled to a temperature below the water dew point to form a mixed-phase material R2P-VB-2 containing a gas phase and a liquid phase;

[0504] The mixed phase material R2P-VB-2 comprises an aqueous phase in which an ammonia component is dissolved.

[0505] In the present invention, usually, (3) the quenching logistics KS is quenching hydrogen-rich gas and / or quenching oil and / or quenching water.

[0506] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0507] The quenching logistics KS is quenching hydrogen-rich gas based on cold high-fraction gas S7-V, and / or quenching oil based on cold high-fraction oil S7-L, and / or quenching water based on cold high-fraction water S7-W.

[0508] In the present invention, generally, (3) the hydrocarbon hydrogenation reaction process R1, the raw hydrocarbon R1F is a distillation oil obtained by separating the oil generated by the direct liquefaction reaction of coal hydrogenation, the hydrocarbon hydrogenation reaction process R1 undergoes a partial hydrogenation saturation reaction of bicyclic aromatic hydrocarbons and / or polycyclic aromatic hydrocarbons, and the hydrogen supply index of the hydrocarbons with a conventional boiling point higher than 200° C. in the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is higher than the hydrogen supply index of the hydrocarbons with a conventional boiling point higher than 200° C. in the raw hydrocarbon R1F;

[0509] The hydrocarbon oil rich in hydrogen-donating hydrocarbon obtained by separating the hydrogenation reaction effluent R1P is used as a hydrogen-donating solvent and prepared with coal powder to form an oil-coal slurry, which is converted into the coal hydrogenation direct liquefaction reaction effluent through a coal hydrogenation direct liquefaction reaction process;

[0510] Separating the effluent from the direct liquefaction reaction of coal hydroprocessing to obtain a distillate oil based on the oil produced by the direct liquefaction of coal hydroprocessing, and using it as the feedstock oil R1F of the hydrocarbon hydrogenation reaction process R1;

[0511] The process of separating the effluent from the direct liquefaction reaction of coal hydroprocessing obtains the initial phenol-containing and aromatic-containing wastewater;

[0512] Based on the initial phenol-containing and aromatic-containing wastewater, the first wastewater is obtained.

[0513] The present invention, usually, (1) the first sewage source

[0514] The first sewage, with or without solid particles, is sewage that has undergone a sewage pretreatment process;

[0515] The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal.

[0516] In the present invention, usually, (i) the first sewage is an aqueous solution containing phenol and aromatic hydrocarbons and contains chloride ions and / or fluoride ions.

[0517] The present invention, generally, (2) sewage gasification process U2

[0518] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0519] In the cooling and condensing process U203, the first sewage vaporized gas U2V-1 is separated into water-dry gas U203-V and condensed oil U203-L.

[0520] In the present invention, usually, during the heating process U204, the water-dry gas U203-V absorbs heat and heats up to become the preheated gas U203-V2;

[0521] The preheated gas U203-V2 enters the hydrogenation purification reaction process R2.

[0522] The present invention, generally, (2) sewage gasification process U2

[0523] The first sewage vaporization gas U2V-1 is a material containing dust and / or high-boiling-point phenol and / or high-boiling-point aromatic hydrocarbons;

[0524] In the oil washing liquid process KU52, the gas based on the first sewage vaporization gas U2V-1 contacts with the washing oil KU52-LF at least once to obtain the washed gas KU52-VP and washed oil KU52-LP with lower dust content and / or lower high-boiling phenol content and / or lower high-boiling aromatic hydrocarbon content, and the washed gas enters the hydrogenation purification reaction process R2;

[0525] At least a part of the wash oil KU52-LF comes from the condensed oil separated in the separation process before the washed gas KU52-VP enters the hydropurification reaction process R2, or comes from the hydrocarbon oil obtained by separating the hydropurification reaction effluent R2P.

[0526] In the present invention, (3) in the hydrogenation purification reaction process R2, two parallel-operated first branch hydrogenation purification reaction processes R2B1 and second branch hydrogenation purification reaction processes R2B2 may be provided;

[0527] When the catalyst operating conditions of the first branch hydrogenation purification reaction process R2B1 are in the final state, most to all of the materials entering the first branch hydrogenation purification reaction process R2B1 are introduced into the second branch hydrogenation purification reaction process R2B2 for hydrogenation purification reaction to extend the continuous operation period.

[0528] In the present invention, (3) in the hydrogenation purification reaction process R2, two parallel-operated first branch hydrogenation purification reaction processes R2B1 and second branch hydrogenation purification reaction processes R2B2 may be provided;

[0529] When the catalyst operating conditions of the first branch hydrogenation purification reaction process R2B1 are in the final state, all materials entering the first branch hydrogenation purification reaction process R2B1 are introduced into the second branch hydrogenation purification reaction process R2B2 for hydrogenation purification reaction, and the first branch hydrogenation purification reaction process R2B1 is isolated from the feed system of the upstream logistics U2V-1B, but hot hydrogen-rich gas is introduced for flow to maintain the operating temperature of the first branch hydrogenation purification reaction process R2B1 within a reasonable range.

[0530] In the present invention, (3) in the hydrogenation purification reaction process R2, two and / or more catalyst beds operated in series may be provided to constitute two or more sub-area hydrogenation purification reaction processes operated in series;

[0531] According to the time course, in the first stage, the logistics U2V-1B passes through the first sub-zone hydrogenation purification reaction process R201, while ensuring that at least hot hydrogen-rich gas flows through the other sub-zones to maintain the operating temperature within a reasonable range;

[0532] According to the time course, in the second stage, when the catalyst operating conditions of the first sub-area hydrogenation purification reaction process R201 are in the final state, part to all of the logistics U2V-1B entering the first hydrogenation purification reaction process R201 is introduced into the second sub-area hydrogenation purification reaction process R202 for hydrogenation purification reaction, and then it is ensured that at least hot hydrogen-rich gas flows through the first sub-area hydrogenation purification reaction process R201 to maintain the temperature of the first hydrogenation purification reaction process R201 within a reasonable range;

[0533] When the hydrogenation purification reaction process R2 is provided with 3 or more catalyst beds operated in series, according to the time course, in the third stage, when the catalyst operating conditions of the second sub-area hydrogenation purification reaction process R202 are in the final state, part to all of the logistics U2V-1B entering the second hydrogenation purification reaction process R202 is introduced into the third sub-area hydrogenation purification reaction process R203 for hydrogenation purification reaction, and then it is ensured that at least hot hydrogen-rich gas flows through the second sub-area hydrogenation purification reaction process R202 to maintain the temperature of the second hydrogenation purification reaction process R202 in a reasonable range;

[0534] By analogy, when the catalyst operating conditions of the last sub-zone hydrogenation purification reaction process R209 are in the final state, a complete operation cycle is completed, and the hydrogenation purification reaction process R2 enters the shutdown step or the first sewage low-load operation step of reducing the first sewage treatment volume.

[0535] In the present invention, usually, (3) in the hydrogenation purification reaction process R2, when the sub-area hydrogenation purification reaction process R20M processes the flow U2V-1B, the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P without passing through other sub-area hydrogenation purification reaction processes;

[0536] At the same time, the sub-area hydrogenation purification reaction processes of the other hydrogenation purification reaction processes R2, except the sub-area hydrogenation purification reaction process R20M, neither receive the logistics U2V-1B nor the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M, and only other hot water-poor hydrogen-rich gases flow through;

[0537] In the reactor of the hydrogenation purification reaction process R2, two or more or all of the sub-area hydrogenation purification reaction processes are arranged in the same pressure equipment shell and the gas phase spaces are interconnected;

[0538] All sub-areas of the hydrogenation purification reaction process R2 are arranged in one or two or more reactors.

[0539] In the present invention, usually, (3) in the first stage of the hydrogenation purification reaction process R2, when the first sub-area hydrogenation purification reaction process R201 processes the flow U2V-1B, the reaction product R201P of the first sub-area hydrogenation purification reaction process R201 is discharged from the hydrogenation purification reaction process R2 after passing through all other sub-area hydrogenation purification reaction processes located downstream, as the hydrogenation purification reaction product R2P;

[0540] When the sub-area hydrogenation purification reaction process R20M processes the flow U2V-1B, the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M passes through the downstream sub-area hydrogenation purification reaction process and is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P;

[0541] At the same time, all sub-area hydrogenation purification reaction processes located upstream of sub-area hydrogenation purification reaction process R20M do not receive logistics U2V-1B, and only other hot water-poor hydrogen-rich gases flow through, and sub-area hydrogenation purification reaction process R20M receives the effluent from the upstream sub-area hydrogenation purification reaction process;

[0542] In the reactor of the hydrogenation purification reaction process R2, two or more or all of the sub-area hydrogenation purification reaction processes are arranged in the same pressure equipment shell;

[0543] All sub-areas of the hydrogenation purification reaction process R2 are arranged in one or two or more reactors.

[0544] In the present invention, generally, the hydrocarbon feed of (3) hydrogenation reaction process R1 comprises one or more of the following fractions:

[0545] ① Hydrocarbons with a conventional boiling point of 200-350°C, including phenols and / or aromatics;

[0546] ② Hydrocarbons with a conventional boiling point of 350-450°C, including phenols and / or aromatics;

[0547] ③ Hydrocarbons with a normal boiling point of 450-550°C, including phenols and / or aromatics;

[0548] The hydrogenation reaction process R1 is a fluidized bed hydrogenation reaction process or a suspended bed hydrogenation reaction process;

[0549] The reaction effluent R1P of the hydrogenation reaction process R1 is a material containing phenols, aromatic hydrocarbons and water.

[0550] In the present invention, generally, the hydrocarbon feed of the hydrogenation reaction process R1 is a hydrocarbon stream obtained by separating the product of the direct liquefaction reaction of coal hydrogenation, and is mainly composed of hydrocarbons with a conventional boiling point of 150 to 550° C., including phenols and aromatic hydrocarbons;

[0551] The hydrogenation reaction process R1 is a fluidized bed hydrogenation reaction process and a suspended bed hydrogenation reaction process;

[0552] The reaction effluent R1P of the hydrogenation reaction process R1 is a material containing phenols, aromatic hydrocarbons and water.

[0553] In the present invention, generally, (2) the operating temperature of the first sewage vaporized gas U2V-1 obtained in the sewage gasification process U2 is at least 30° C. higher than the water dew point;

[0554] ⑶ The operating temperature of the hydrogenation purification reaction process R2 is at least 50°C higher than the water dew point, and the hydrogen partial pressure of the hydrogenation purification reaction process R2 is 6.0-18.0MPa.

[0555] In the present invention, generally, (2) the operating temperature of the first sewage vaporized gas U2V-1 obtained in the sewage gasification process U2 is at least 30° C. higher than the water dew point;

[0556] ⑶ The operating temperature of the hydrogenation purification reaction process R2 is at least 70°C higher than the water dew point, and the hydrogen partial pressure of the hydrogenation purification reaction process R2 is 9.0-14.0MPa.

[0557] In the present invention, usually, (3) in the hot high pressure separation process S1, the reaction effluent R1P of the hydrogenation reaction process R1 is separated to obtain hot high fraction gas S1-V and hot high fraction oil S1-L;

[0558] The hydrocarbon stream S1-L-TOR2 obtained by separating the hot high-fraction oil S1-L enters the hydrogenation purification reaction process R2;

[0559] The hydrocarbon stream S1-L-TOR2 is mainly composed of hydrocarbons with a conventional boiling point below 250°C and / or hydrocarbons with a boiling point of 250-320°C.

[0560] In the present invention, usually, (3) a clean hydrocarbon stream KEYS containing hydrocarbon components with a conventional boiling point of 300-350°C is subjected to a hydrogenation purification reaction process R2, and at least a portion of the clean hydrocarbon stream KEYS is maintained in a liquid phase during the hydrogenation purification reaction process R2.

[0561] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0562] Based on the cold high-pressure separation process feed of the hydrogenation purification reaction effluent R2P, it flows out of the last heat exchanger K-HX for heat recovery to become the logistics K-HX-HP, and the weight flow rate of the liquid water component in the logistics K-HX-HP is not less than 85% of the weight flow rate of the water component in the cold high-pressure water separation S7-W;

[0563] Logistics K-HX-HP, after being cooled in the cooling process, enters the cold high-pressure separation process S7.

[0564] In the present invention, usually, (3) in the cold high pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L;

[0565] Based on the cold high-pressure separation process feed of the hydrogenation purification reaction effluent R2P, it flows out of the last heat exchanger K-HX for heat recovery to become the logistics K-HX-HP, and the temperature of the logistics K-HX-HP is not higher than 150-170℃;

[0566] Logistics K-HX-HP, after being cooled in the cooling process, enters the cold high-pressure separation process S7.

[0567] In the present invention, (2) the washing oil U3-AL may be a heavy diesel component having a conventional boiling point of 250 to 350°C.

[0568] In the present invention, (2) the washing oil KU52-LF can be a heavy diesel component having a conventional boiling point of 250 to 350°C.

[0569] The present invention can be operated in the following manner: (1) the first sewage source

[0570] The first sewage includes sewage containing phenol, aromatic hydrocarbons and solid particles generated from the separation process of coal hydrogenation direct liquefaction reaction products, and is sewage that has undergone or has not undergone sewage pretreatment;

[0571] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0572] (2) Washing oil KU52-LF is a heavy diesel component with a conventional boiling point of 250-350°C. It is heavy diesel DIES100 distilled from the oil generated by the hydrogenation modification reaction of "coal hydrogenation direct liquefaction oil and / or hydrogenation modified oil of coal hydrogenation direct liquefaction oil", or it is the rich absorption oil formed by the heavy diesel DIES100 through the recovery of liquefied gas and gasoline containing liquefied gas and light gasoline components. In this way, heavy diesel DIES100 can be used twice in series.

[0573] The present invention can be operated in the following manner: (1) the first sewage source

[0574] The first sewage includes sewage containing phenol, aromatic hydrocarbons and solid particles generated from the separation process of coal hydrogenation direct liquefaction reaction products, and is sewage that has undergone or has not undergone sewage pretreatment;

[0575] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0576] (2) Washing oil KU52-LF is a heavy diesel component with a conventional boiling point of 250-350°C. It is heavy diesel DIES100 distilled from the oil generated by the hydrogenation modification reaction of "coal hydrogenation direct liquefaction oil and / or hydrogenation modified oil of coal hydrogenation direct liquefaction oil", or it is the rich absorption oil formed by the heavy diesel DIES100 through the recovery of liquefied gas and gasoline containing liquefied gas and light gasoline components. In this way, heavy diesel DIES100 can be used twice in series.

[0577] The present invention can be operated in the following manner: (1) the first sewage source

[0578] The first sewage, containing or not containing solid particles, is the sewage of the initial sewage with or without the sewage pretreatment process;

[0579] The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process;

[0580] ⑵ Wastewater gasification process U2

[0581] In the first sewage light oil desolidification process, the first sewage is mixed with the first desolidified hydrocarbon oil feedstock and separated into the first desolidified oil-rich sewage and the first solid-reduced sewage;

[0582] The solid content in the first desolidified rich oil is higher than the solid content in the first desolidified hydrocarbon oil feedstock;

[0583] The solid content in the first solids-reducing sewage is lower than the solid content in the first sewage;

[0584] In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM including water, phenol and / or aromatic hydrocarbons in the first solid reduction sewage is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V;

[0585] The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas;

[0586] The first sewage vaporized gas U2V-1 may contain or may not contain liquid hydrocarbon oil.

[0587] The present invention may be operated in the following manner: (2) in the first sewage light oil desolidification process, the first desolidified hydrocarbon oil feedstock is a hydrocarbon oil based on the condensed oil of the sewage gasification process U2, and / or is a hydrocarbon oil obtained by separating the effluent R2P of the hydrogenation purification reaction;

[0588] The first solids are removed and the oil is enriched, and then the solids are washed with oil before entering the solids removal process before the hydrogen sulfide removal and deammoniation process;

[0589] In the pre-solids removal process before the dehydrogensulfurization and deammoniation process, the first desolids-rich oil-rich logistics is mixed and contacted with the pre-wastewater logistics based on the initial wastewater to separate into pre-solids-rich oil-rich and pre-solids-reduced wastewater;

[0590] The solid content in the pre-solidification rich oil is higher than the solid content in the first desolidification rich oil;

[0591] The solid content in the front solids reduction sewage is lower than the solid content in the front sewage stream;

[0592] Based on the logistics of the pre-solid reduction sewage, it goes through the first sewage light oil desolidification process.

[0593] The present invention may be operated in such a manner that (3) the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-fraction separation process R1P-S1; the hot high-fraction oil R1P-S1L contains solid particles;

[0594] The logistics based on the hot high-fraction gas R1P-S1V is mixed and contacted with the logistics based on the first sewage to form a water-dry or water-wet first sewage vaporized gas U2V-1;

[0595] In the separation and fractionation process FRAC80, the hot high fraction oil R1P-S1L is separated into gas, narrow fraction oil products, and separation bottom oil FRAC80-DV containing solid particles;

[0596] The oil-rich logistics based on the pre-solid removal enters the separation and fractionation process FRAC80 and is mixed with the logistics based on the thermal high oil separation R1P-S1L to separate into narrow-fraction oil products. The solid particles contained in the oil-rich logistics based on the pre-solid removal enter the separation bottom oil FRAC80-DV.

[0597] The present invention may be operated in the following manner: (3) in the hydrogenation purification reaction process R2, other hydrocarbons P600 mainly composed of phenols and / or aromatics having a conventional boiling point below 350° C. are processed in combination;

[0598] Hydrocarbons P600, including or not including the hydrocarbon stream obtained by separating the oil produced by direct liquefaction of coal.

[0599] The present invention may be operated in the following manner: (3) in the hydrogenation purification reaction process R2, other hydrocarbons P700 mainly composed of phenols and / or aromatics having a conventional boiling point below 250° C. are processed jointly;

[0600] Hydrocarbons P700, including or not including the hydrocarbon stream obtained by separating the oil produced by direct liquefaction of coal.

[0601] The present invention may be operated in such a manner that (3) the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1;

[0602] The hot high-fraction oil R1P-S1L is separated and mainly contains phenol and / or aromatic hydrocarbons with a conventional boiling point below 250°C, which enter the hydrogenation purification reaction process R2 for joint processing.

[0603] The present invention can be operated in the following manner: (i) the first sewage source is sewage with low chloride ion content, selected from the top water of the distillation tower and the vacuum tower of the oil generated by direct liquefaction of coal by hydrogenation, the top water of the distillation tower of the oil generated by hydrogenation modification of direct liquefaction of coal by hydrogenation, and the acidic water of gas fractionation.

[0604] The present invention may be operated in the following manner: (3) hydrocarbon hydrogenation reaction process R1 is a hydrogenation and upgrading reaction process of coal direct liquefaction oil or coal direct liquefaction oil hydrogenation and modification oil.

[0605] The present invention can be operated in the following manner: (2) Sewage gasification process U2

[0606] The first sewage vaporized gas U2V-1 is a material containing dust and / or high-boiling-point phenols and / or high-boiling-point aromatic hydrocarbons. The gas based on the first sewage vaporized gas U2V-1 undergoes a cooling, condensation, separation and deliquescence process KU51 and / or an oil eluent process KU52 to obtain a gas with a lower dust content and / or a lower high-boiling-point phenol content and / or a lower high-boiling-point aromatic hydrocarbon content and enters the hydrogenation purification reaction process R2.

[0607] Example

[0608] This embodiment includes a hydrocarbon hydrogenation reaction process R1, a hot high-pressure separation process R1P-S1 of the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1, a wastewater spray gasification process WDV, a first oil washing process U3, a hydrogenation purification reaction process R2, a heat recovery and cooling process of the hydrogenation purification reaction effluent R2P including a heat recovery heat exchanger K-HX, a heat dissipation and cooling process, and a cold high-pressure separation process S7.

[0609] Each step is described in detail below.

[0610] The effluent of the coal hydrogenation direct liquefaction reaction of the coal hydrogenation direct liquefaction device is separated into coal liquefaction hot high-fraction gas and coal liquefaction hot high-fraction oil through a coal liquefaction hot high-pressure separation process, and the coal liquefaction hot high-fraction gas is separated into coal liquefaction temperature high-fraction gas and coal liquefaction temperature high-fraction oil through a coal liquefaction temperature high-pressure separator, an oil washing section is arranged at the upper part of the coal liquefaction temperature high-pressure separator, and the coal liquefaction temperature high-fraction gas is washed with a light diesel oil fraction, and the coal liquefaction temperature high-fraction gas is injected with water, condensed and cooled, and separated into coal liquefaction cold high-fraction gas, coal liquefaction cold high-fraction oil and coal liquefaction cold high-fraction water through a coal liquefaction cold high-pressure separator; in a coal liquefaction cold high-fraction water low-pressure flash tank, the coal liquefaction cold high-fraction water after pressure reduction is depressurized to remove dissolved gas and entrained oil to obtain initial phenol-containing and aromatics-containing wastewater.

[0611] Table 5 is the pollutant composition table of the initial phenol-containing and aromatic hydrocarbon-containing wastewater.

[0612] The initial phenol-containing and aromatic hydrocarbon-containing wastewater with a composition as shown in Table 5 is subjected to a wastewater pretreatment process to obtain a first wastewater, and the wastewater pretreatment process includes the following functions: solid removal by a filter, free oil removal by a cyclone, solid removal and oil extraction by an oil washing method, hydrogen sulfide and carbon dioxide removal by a stripping tower, and ammonia removal by a stripping tower, without being subjected to an extraction and dephenolization process.

[0613] Table 5 Pollutant composition of initial phenol-containing and aromatic hydrocarbon-containing wastewater

[0614]

[0615] Table 6 Pollutant composition of the first sewage (pre-treated sewage of high-concentration coal liquefaction sewage after desulfurization and deamination but without dephenolization)

[0616]

[0617] The hydrocarbon feed F01 of the hydrogenation reaction process R1 is 436.628 tons / hour of hydrocarbon flow obtained by separating the products of direct liquefaction reaction of coal hydrogenation, which is mainly composed of hydrocarbons with a conventional boiling point of 50-550°C, containing phenols and aromatic hydrocarbons, and carrying about 250 ppm of solid particles; the hydrogenation reaction process R1 is an ebullating bed hydrogenation modification reaction process; the reaction effluent R1P of the hydrogenation reaction process R1 is a material containing phenols, aromatic hydrocarbons, water vapor and solid particles.

[0618] The operating conditions of the hydrocarbon hydrogenation reaction process R1 are: the reactor outlet pressure is 16.60MPa, the hydrogen partial pressure is not less than 11.4MPaA, and the temperature is 383.8°C; the hydrogen supply index of hydrocarbons with a normal boiling point higher than 200°C in the reaction effluent R1P is 24.5mgHnβ / g solvent, which is 7.5mgHnβ / g higher than the hydrogen supply index of 17.0mgHnβ / g solvent of hydrocarbons with a normal boiling point higher than 200°C in the raw hydrocarbon R1F.

[0619] The operating conditions of the hydrogenation purification reaction process R2 are: pressure of 16.26MPa, hydrogen partial pressure not less than 9.56MPaA, temperature of 380℃, total gas phase feed volume flow rate of 217973Nm 3 / t, warm high-pressure oil 18.941 tons / hour, cold high-pressure oil 10.487 tons / hour, hydrogen-to-oil ratio 7406Nm 3 / t, the hourly space velocity of all 4 hydrogenation purification catalyst liquids is 0.20h -1 The liquid hourly space velocity of each hydrogenation purification catalyst bed is 0.80h -1 .

[0620] The reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1; the hot high-pressure separation process R1P-S1 is carried out in the hot high-pressure separator S1E (not shown), and its operating conditions are: pressure of 16.60MPa and temperature of 383.8℃.

[0621] The hot high-fraction gas R1P-S1V contains ammonia, hydrogen sulfide, hydrogen chloride, water, phenol, and aromatic hydrocarbons. According to conventional processes, it needs to be washed with water, and then cooled by a high-pressure air cooler and enters a hydrogenation-modified cold high-fraction gas separator to separate hydrogenation-modified cold high-fraction water. The hydrogenation-modified cold high-fraction water is also acidic wastewater containing phenol, aromatic hydrocarbons, and chloride ions. According to the present invention, this part of the acidic wastewater containing phenol and aromatic hydrocarbons can be eliminated and converted into acidic water with low organic toxicity that is easy to be simply biochemically treated to purify organic matter.

[0622] The hot high-fraction gas R1P-S1V, after being heated to 430°C by the heating furnace GF1, becomes the hot high-fraction gas MSV1 after the furnace; the hot high-fraction gas MSV1 after the furnace enters the sewage gasification oil washing tower T1, and as a heat carrier and a carrying gas for the vaporized water, heats and vaporizes the first sewage sprayed into the air flow in three batches to form the vaporized gas U2V-1 of the water-dry first sewage, and the process simulation calculation is based on single-stage mixed flash evaporation treatment; at the same time, the condensed oil WDV-L generated by the cooling of the hot high-fraction gas MSV1 after the furnace is used as an adsorbent and carrying agent for the solid dust remaining after the first sewage is vaporized, and is discharged from the bottom of the sewage gasification oil washing tower T1.

[0623] The sewage gasification oil washing tower T1 can be split into several gas-liquid contactors for operation, and the temperature difference between the inlet temperature and the outlet temperature of a single device should not be too large.

[0624] The first sewage with a pressure of 17.0MPa and a temperature of 145°C is divided into three parallel sewage paths FW02, FW03, and FW04, which enter the sewage gasification section in the sewage gasification oil washing tower T1 and are sprayed into the air flow from different positions.

[0625] Five anti-blocking packing layers INC01, INC02, INC03, INC04 and INC05 are arranged in the sewage gasification oil washing tower T1 to disperse the liquid and gas, increase the surface area of ​​the liquid phase, and provide the gas-liquid contact area. The anti-blocking packing itself also has the heat transfer function of the heat exchanger.

[0626] The packing layers INC01, INC02 and INC03 are used to receive three types of sewage FW02, FW03 and FW04.

[0627] Packing layer INC04, used to receive circulating washing oil WDV-L3.

[0628] The packing layer INC05 is used to receive the sprayed and dispersed washing oil U3-AL entering the sewage gasification oil washing tower T1, and countercurrently contact with the vaporized gas U2V-1 of the first sewage to obtain the first washed gas U3-PV and the first washed oil U3-PL.

[0629] After the first wash, the oil U3-PL flows downward and can be discharged from the sewage gasification oil washing tower T1, but usually enters the packing layer INC04 and is mixed with the circulating washing oil WDV-L3 for secondary use.

[0630] The condensed oil WDV-L is divided into parallel WDV-L1 and WDV-L2. WDV-L1 enters the separation and distillation process FRAC80. WDV-L2 is pressurized by pump T1PUMP and enters the sewage gasification oil washing tower T1 as material WDV-L3 to be sprayed and dispersed into the packing layer INC04.

[0631] Table 7 is a table showing the composition of the aqueous stream.

[0632] In Table 7, in order to conservatively design the hydrogenation purification reaction process R2, it is assumed that all CO and CO2 in the hydrocarbon feed F01 of the hydrogenation reaction process R1 are not hydrogenated and converted. In order to simplify the calculation, the first sewage is considered as pure water for process simulation.

[0633] The first washing oil can be heavy diesel DIES100 fractionated from the oil generated by the hydrogenation and modification reaction of "coal hydrogenation direct liquefaction oil and / or hydrogenation and modification oil product of coal hydrogenation direct liquefaction oil", or it can be the rich absorption oil formed by the heavy diesel DIES100 through the recovery of liquefied gas and gasoline absorption process of gas containing liquefied gas and light gasoline components, so that the heavy diesel DIES100 can be used in series twice.

[0634] The first washed gas U3-PV is heated to 370°C by the heating furnace GF1 and then enters the hydrogenation purification reaction process R2 as logistics U2V-1B.

[0635] Table 7 Composition of water-containing stream

[0636]

[0637] The hydrogenation purification reaction process R2 is carried out in the hydrogenation purification reactor R2E.

[0638] In order to extend the operation period, the hydrogenation purification reactor R2E is provided with four hydrogenation purification catalyst beds of the same type, quantity and configuration mode, which are operated in series, and constitute four sub-area hydrogenation purification reaction processes R201, R202, R203 and R204, which are operated in series. The operation mode is as follows:

[0639] ① In the first stage, when the first sub-area hydrogenation purification reaction process R201 processes the flow U2V-1B, the reaction product R201P of the first sub-area hydrogenation purification reaction process R201 passes through all other sub-area hydrogenation purification reaction processes R202, R203, and R204 located downstream and then is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P;

[0640] Logistics U2V-1B is transported as logistics U2V-1B1 into hydrogenation purification reaction process R2;

[0641] ② In the second stage, when the catalyst operating conditions of the first sub-area hydrogenation purification reaction process R201 are in the final state, part to all of the logistics U2V-1B entering the first hydrogenation purification reaction process R201 is introduced into the second sub-area hydrogenation purification reaction process R202 for hydrogenation purification reaction, and then at least hot hydrogen-rich gas is ensured to flow through the first sub-area hydrogenation purification reaction process R201 to maintain the temperature of the first hydrogenation purification reaction process R201 within a reasonable range;

[0642] The reaction product R202P of the second sub-area hydrogenation purification reaction process R202 is discharged from the hydrogenation purification reaction process R2 after passing through all other sub-area hydrogenation purification reaction processes located downstream, as the hydrogenation purification reaction product R2P;

[0643] Logistics U2V-1B is transported as logistics U2V-1B2 into hydrogenation purification reaction process R2;

[0644] ③ In the third stage, when the catalyst operating conditions of the second sub-area hydrogenation purification reaction process R202 are in the final state, part to all of the logistics U2V-1B entering the second hydrogenation purification reaction process R202 is introduced into the third sub-area hydrogenation purification reaction process R203 for hydrogenation purification reaction, and then at least hot hydrogen-rich gas is ensured to flow through the second sub-area hydrogenation purification reaction process R202 to maintain the temperature of the second hydrogenation purification reaction process R202 within a reasonable range;

[0645] The reaction product R203P of the third sub-zone hydrogenation purification reaction process R203 passes through the fourth sub-zone hydrogenation purification reaction process R204 located downstream and then is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P;

[0646] Logistics U2V-1B is transported as logistics U2V-1B3 into hydrogenation purification reaction process R2;

[0647] ④ In the fourth stage, when the catalyst operating conditions of the third sub-area hydrogenation purification reaction process R203 are in the final state, part to all of the logistics U2V-1B entering the third hydrogenation purification reaction process R203 is introduced into the fourth sub-area hydrogenation purification reaction process R204 for hydrogenation purification reaction, and then at least hot hydrogen-rich gas is ensured to flow through the third sub-area hydrogenation purification reaction process R203 to maintain the temperature of the third hydrogenation purification reaction process R202 within a reasonable range;

[0648] The reaction product R204P of the fourth sub-zone hydrogenation purification reaction process R204 is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P;

[0649] Logistics U2V-1B is transported as logistics U2V-1B4 into hydrogenation purification reaction process R2;

[0650] ⑤ Until the catalyst operating conditions of the fourth sub-area hydrogenation purification reaction process R204 are in the final state, a complete operation cycle is completed, and the hydrogenation purification reaction process R2 enters the shutdown step or the first sewage low-load operation step of reducing the first sewage treatment volume.

[0651] Flushing hydrogen BH03 is divided into 4 parallel routes: flushing hydrogen BH031, flushing hydrogen BH03, flushing hydrogen BH033, and flushing hydrogen BH034. Flushing hydrogen BH03 is used to replace the medium and can also be used to maintain the temperature of the catalyst bed being flushed.

[0652] The valve VALVE is used to cut off the flow of goods or adjust the flow rate of goods.

[0653] The reaction indexes of hydrogenation purification reaction process R2 are as follows:

[0654] The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 99.5%;

[0655] The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 98.5%;

[0656] The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 99.8%;

[0657] In the hydrogenation purification reaction process R2, the hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon reduces the aromatic carbon ratio by more than 70%;

[0658] The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 90%;

[0659] The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 97%;

[0660] The weight content of hydrocarbon components having a normal boiling point higher than 280° C. in the hydropurification reaction effluent R2P is less than 25 weight %;

[0661] The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 7 weight %;

[0662] The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 3 weight %.

[0663] The hydrogenation purification reaction effluent R2P passes through the heat exchangers HX31AB, HX32, HX33, HX34, K-HX, and HX36 for cooling, and then enters the cold high-pressure separator S7E.

[0664] The effluent R2P of the hydrogenation purification reaction passes through the heat exchanger HX31AB and then releases heat and cools down to 270°C to become material R2P1. At the same time, the hydrocarbon feed F01 of the 260.5°C hydrogenation reaction process R1 passes through the heat exchanger HX31AB and then absorbs heat and heats up to 307.0°C to become the hot hydrocarbon feed F02.

[0665] Use circulating warm high-pressure water with a flow rate of 20 t / h to rapidly cool it to a temperature below the water dew point temperature of 252.5 water dew point ℃, forming 17.516 t / h of liquid water phase, which is then cooled to 200 ℃ through a heat exchanger and enters a warm and high-pressure separator to separate into warm high-pressure gas, warm high-pressure oil and warm high-pressure water.

[0666] After material R2P1 is mixed with 20t / h of circulating high-temperature water, its temperature is rapidly cooled from 270℃ to 252.5℃ to become logistics R2P2 containing 17.516t / h of liquid water. Material R2P2 releases heat and cools down to 252.5℃ through heat exchanger HX32 to become material R2P3. At the same time, the mixed hydrogen MH2 at 164.8℃ absorbs heat and rises to 226.4℃ through heat exchanger HX32 to become mixed hydrogen MH4.

[0667] Material R2P3 passes through the heat exchanger HX33 and then releases heat and cools down to 200.0℃ to become material R2P4. At the same time, the deoxygenated water passes through the steam generator HX33 and absorbs heat (heat load 16.96MW) to heat up and generate 1.0Ma of saturated water vapor.

[0668] The warm high pressure separation process WHPS is carried out in the cold high pressure separator WHPS-E, and its operating conditions are: pressure of 16.07MPa, temperature of 200℃, and the separated material R2P4 is obtained to obtain warm high pressure gas separation WHPS-V, warm high pressure oil separation WHPS-L, and warm high pressure water separation WHPS-W.

[0669] As shown, the warm high separation water WHPS-W is divided into two routes, one is used as 20t / h circulating warm high separation water WHPS-WRLR1, which is pressurized by the circulating pump W-PUMP as logistics WHPS-WR2 to cool logistics R2P1, and the other is used as 28.714t / h warm high separation water net product WHPS-W1 to enter the heat exchanger K-HX.

[0670] The warm high pressure oil separation WHPS-L goes to the distillation tower after the pressure reduction and degassing process.

[0671] The warm high-pressure gas WHPS-V and the warm high-pressure water WHPS-W1 are mixed to form logistics R2P7, which is cooled to 160.0℃ by heat release in the heat exchanger K-HX to become material K-HX-HP. At the same time, the mixed hydrogen MH1 at 75.8℃ is heated to 164.8℃ by heat absorption in the heat exchanger K-HX to become mixed hydrogen MH2.

[0672] Material K-HX-HP is mixed with quench material WW2 (water injection for emergency, not used in normal operation) to become material R2P9. Material R2P9 is cooled to 54°C by air cooler HX35 to release heat (heat load 16.34MW) and become material R2P10.

[0673] The cold high-pressure separation process S7 is carried out in the cold high-pressure separator S7E, and its operating conditions are: pressure of 15.87MPa, temperature of 54°C, and the separated material R2P9 obtains cold high-fraction gas S7V, cold high-fraction oil S7L, and 45.010t / h cold high-fraction water S7W (containing 42.331t / h of water).

[0674] The hydrogenation purification reaction effluent R2P passes through the last heat exchanger K-HX for heat recovery and becomes a stream K-HX-HP with a temperature of 160°C. The weight flow rate of the liquid water component in the stream K-HX-HP is 37.342 t / h, which is 88.2% of the weight flow rate of the water component in the cold high-cut water S7W of 42.320 t / h.

[0675] The cold high-fraction gas S7V becomes circulating hydrogen S7V1 after being compressed by the circulating hydrogen compressor CE2; the new hydrogen FH1 becomes new hydrogen FH2 after being compressed by the new hydrogen compressor CE1; the new hydrogen FH2 is mixed with the circulating hydrogen S7V1 to become mixed hydrogen MH1.

[0676] Mixed hydrogen MH4 is divided into three parallel routes: mixed hydrogen MH41, mixed hydrogen MH42, and mixed hydrogen MH43.

[0677] The mixed hydrogen MH41 and the hot hydrocarbon feed F02 are mixed into the mixture MF1, and the mixture MF1 is mixed with liquid sulfur into the mixture MF2; the mixture MF is heated by the heating furnace GF2 to become the hot mixture MF3 and enters the first reaction stage of the hydrocarbon hydrogenation reaction process R1D.

[0678] The mixed hydrogen MH42 is heated in the heating furnace GF2 to become hot mixed hydrogen R1INH and enters the second reaction stage of the hydrocarbon hydrogenation reaction process R1.

[0679] The mixed hydrogen MH43 is heated in the heating furnace GF2 to become hot mixed hydrogen BH00. The hot mixed hydrogen BH00 is divided into three parallel routes for use: gas lift hydrogen BH01, gas lift hydrogen BH02, and purge hydrogen BH03.

[0680] In the separation and distillation process FRAC80, the hot high-fraction oil R1P-S1L and the condensate oil WDV-L1 are separated into narrow-fraction oil products: naphtha 80L1 mainly composed of conventional liquid hydrocarbons with a conventional boiling point below 140°C, gas oil 80L2 mainly composed of conventional liquid hydrocarbons with a conventional boiling point of 140-330°C, middle-fraction hydrogen-donating solvent oil 80L3 mainly composed of conventional liquid hydrocarbons with a conventional boiling point of 230-400°C, and heavy-fraction hydrogen-donating solvent oil 80L4 mainly composed of conventional liquid hydrocarbons with a conventional boiling point of 280-550°C.

[0681] The heavy fraction hydrogen supply solvent oil 80L4 is divided into 1 routes for use: the first route of heavy fraction hydrogen supply solvent oil 80L42 leaves the device to configure coal slurry, and the second route of heavy fraction hydrogen supply solvent oil 80L41 is pressurized by a pump and returned to the hydrocarbon hydrogenation reaction process R1 for cyclic hydrogenation reaction to increase the hydrogen supply index of the externally delivered heavy fraction hydrogen supply solvent oil 80L42.

[0682] Table 8 is the flash phase equilibrium data curve of the hydrogenation purification reaction effluent R2P.

[0683] As can be seen from Table 8, the oil dew point temperature of the hydrogenation purification reaction effluent R2P is about 293.41°C, and the water dew point temperature is about 249.78°C. In order to prevent the occurrence of a chloride ion high-concentration aqueous phase or avoid or reduce the area where a chloride ion high-concentration aqueous phase exists, the material R2P needs to be mixed with the quenching material XF to reduce the temperature below the water dew point and form a large amount of liquid water. The source of the quenching material XF is not limited. The present invention adopts a method of circulating high-temperature water separation to change the phase equilibrium and increase the dew point temperature. The problem is solved by making the temperature reduction of the material R2P very small, thereby economically recovering heat.

[0684] Table 9 is the flash phase equilibrium data curve of the dew point temperature of the logistics R2P2 after high water separation at the circulating temperature.

[0685] Table 10 shows the distillation curves of warm high fraction oil WHPS-L and cold high fraction oil S7L.

[0686] According to the method of the present invention, the dew point temperature of the logistics after the injection of circulating high temperature water is increased to 266.84°C, which is 17.06°C higher than the dew point temperature in Table 8.

[0687] It can be seen from Tables 7 and 10 that clean heavy diesel washing oil U3-AL is used to wash the vaporized gas U2V-1. The heavy diesel washing oil U3-AL, as an absorption oil, absorbs some high-boiling-point hydrocarbons containing pollutant components in the washed vaporized gas U2V-1, thereby purifying the vaporized gas U2V-1. This is equivalent to replacing some high-boiling-point hydrocarbons containing pollutant components in the vaporized gas U2V-1 with clean heavy diesel, which is beneficial to reducing the hydrogen partial pressure of the hydrogenation purification reaction process R2, increasing the liquid space velocity of the hydrogenation purification catalyst, and reducing the amount of catalyst used.

[0688] As can be seen from Table 10, the main functions of the warm and high pressure separator are as follows:

[0689] ① Condensation produces warm high-fraction oil net products, thereby reducing the content of high-boiling-point hydrocarbon components in cold high-fraction oil, which is beneficial to reducing the distillation dry point in cold high-fraction water, reducing the deoiling task in the subsequent purification process of cold high-fraction water, and reducing the digestion load of the biochemical process;

[0690] ② Retain the heat energy of the net product of high-temperature oil separation, reduce the heat dissipation load of the high-pressure air cooler, and improve the heat recovery rate.

[0691] Table 8 Flash phase equilibrium data curve of hydrogenation purification reaction effluent R2P

[0692]

[0693]

[0694] Table 9 Flash phase equilibrium data curve of the dew point temperature of the circulation temperature high water separation logistics R2P2

[0695]

[0696]

[0697] Table 10 Distillation curves of warm high-fraction oil WHPS-L and cold high-fraction oil S7L

[0698]

Claims

1. A method for hydrogenating and purifying evaporated gas from wastewater containing phenol and / or aromatic hydrocarbons, characterized in that The following steps are involved: The pollutant components KC contained in the first sewage include phenol and / or aromatic hydrocarbons, include or exclude solid particles, and include or exclude other pollutant components that can undergo hydrogenation conversion reactions in the hydrogenation purification reaction process R2 to reduce their molecular electrical conductivity; The heteroatom-containing organic matter includes oxygen-containing organic matter, includes or excludes nitrogen-containing organic matter, includes or excludes sulfur-containing organic matter, includes or excludes chlorine-containing organic matter; In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content; In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to produce organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to produce aromatic hydrocarbons with a lower aromatic carbon rate.

2. The method according to claim 1, characterized in that: ⑴The first source of sewage The first sewage, containing or not containing solid particles, is sewage that has or has not undergone a sewage pretreatment process; The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process; ⑵ Wastewater gasification process U2 In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V; The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas; The first sewage vaporized gas U2V-1 contains or does not contain liquid hydrocarbon oil; ⑶ Hydrogenation purification reaction process R2 In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content; In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate; The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

3. The method according to claim 2, characterized in that: ⑴The first source of sewage The source of the first wastewater includes one or more of the following processes: coal hydrogenation direct liquefaction process, coal gasification process, coal dry distillation process, coal tar processing process; The first sewage, containing solid particles, is sewage that has or has not undergone a sewage pretreatment process; The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal; ⑵ Wastewater gasification process U2 In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V; The first sewage vaporization gas U2V-1 is water dry gas; The first sewage vaporized gas U2V-1 contains liquid hydrocarbon oil; ⑶ Hydrogenation purification reaction process R2 In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the water-dry stream U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content; In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate; The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

4. The method according to claim 2, characterized in that: ⑴The first source of sewage The first sewage, containing or not containing solid particles, is sewage that has or has not undergone a sewage pretreatment process; The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal; ⑵ Wastewater gasification process U2 In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V; The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas; The first sewage vaporized gas U2V-1 contains or does not contain liquid hydrocarbon oil; ⑶ Hydrocarbon hydrogenation reaction process R1 and hydrogenation purification reaction process R2 A hydrogen-containing gas phase stream R1P-VB based on the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is subjected to a hydrogenation purification reaction process R2; In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content; In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate; In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics R1P-VB undergoes a hydrogenation refining purification reaction of at least a portion of the pollutant components to be converted into a hydrogenation purification reaction effluent R2P with a low organic pollutant content; In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics R1P-VB undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate; In the hydrogenation purification reaction process R2, the components based on the stream U2V-1B or the intermediate hydrogenation products based on the components of the stream U2V-1B are mixed and contacted with the stream R1P-VB or the intermediate hydrogenation products of the stream R1P-VB; The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

5. The method according to claim 3, characterized in that: ⑴The first source of sewage The source of the first wastewater includes one or more of the following processes: coal hydrogenation direct liquefaction process, coal gasification process, coal dry distillation process, coal tar processing process; The first sewage, containing solid particles, is sewage that has or has not undergone a sewage pretreatment process; The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal; ⑵ Wastewater gasification process U2 In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V; The first sewage vaporization gas U2V-1 is water dry gas; The first sewage vaporized gas U2V-1 contains liquid hydrocarbon oil; ⑶ Hydrocarbon hydrogenation reaction process R1 and hydrogenation purification reaction process R2 A hydrogen-containing gas phase stream R1P-VB based on the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is subjected to a hydrogenation purification reaction process R2; In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics U2V-1B containing the first sewage vaporization gas U2V-1 undergoes a hydrogenation refining purification reaction of at least a portion of the pollutants KC to convert it into a hydrogenation purification reaction effluent R2P with a low organic pollutant content; In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics U2V-1B undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate; In the hydrogenation purification reaction process R2, in the presence of hydrogen, hydrogen sulfide and a hydrogenation purification catalyst, the logistics R1P-VB undergoes a hydrogenation refining purification reaction of at least a portion of the pollutant components to be converted into a hydrogenation purification reaction effluent R2P with a low organic pollutant content; In the hydrogenation purification reaction process R2, at least a portion of the heteroatom-containing organic matter in the logistics R1P-VB undergoes a hydrogenation decontamination reaction to generate organic matter and metal sulfides without heteroatoms, and / or at least a portion of the aromatic ring-containing components in the logistics U2V-1B undergoes an aromatic ring hydrogenation saturation reaction to generate aromatic hydrocarbons with a lower aromatic carbon rate; In the hydrogenation purification reaction process R2, the components based on the stream U2V-1B or the intermediate hydrogenation products based on the components of the stream U2V-1B are mixed and contacted with the stream R1P-VB or the intermediate hydrogenation products of the stream R1P-VB; The hydrogenation purification reaction effluent R2P is separated to obtain a water phase stream.

6. The method according to claim 4, characterized in that: ⑶ The reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is a logistics containing phenol, aromatic hydrocarbons, water and hydrogen.

7. The method according to claim 5, characterized in that: ⑶ The reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is a logistics containing phenol, aromatic hydrocarbons, water and hydrogen.

8. The method according to claim 4, characterized in that: (3) The reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1; The logistics based on the hot high-fraction gas R1P-S1V is mixed and contacted with the logistics based on the first sewage to form water-dry or water-wet first sewage vaporized gas U2V-1.

9. The method according to claim 8, characterized in that: ⑶ Set up the sewage spray gasification process WDV; In the sewage spray gasification process WDV, a liquid water-containing logistics based on the first sewage is sprayed into a gas-containing logistics based on the hot high-fraction gas R1P-S1V for vaporization to form a logistics containing water-dry first sewage vaporized gas U2-2. The operating temperature of the water-dry first sewage vaporized gas U2-2 is lower than the operating temperature of the logistics R1P-S1V, with or without the generation of condensed oil WDV-L.

10. The method according to claim 9, characterized in that: ⑶ In the sewage spray gasification process WDV, condensed oil WDV-L is produced; Condensate oil WDV-L, with or without solid particles from the first sewage.

11. The method according to claim 10, characterized in that: ⑶ In the sewage spray gasification process WDV, the condensed oil WDV-L is separated so that it does not go through the hydrogenation purification reaction process R2.

12. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ In the cold high-pressure separation process S7, the water-containing and hydrogen-containing flow based on the hydrogenation purification reaction effluent R2P is separated to obtain cold high-pressure water separation S7-W.

13. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; At least a portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrogenation purification reaction effluent R2P for recycling.

14. The method according to claim 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; At least a portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrocarbon hydrogenation reaction process R1 for recycling.

15. The method according to claim 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; A portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrocarbon hydrogenation reaction process R1 for recycling; A portion of the hydrogen-rich gas stream based on the cold high-fraction gas S7-V is returned to the hydrogenation purification reaction effluent R2P for recycling without passing through the hydrocarbon hydrogenation reaction process R1.

16. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; The hydrogen concentration in the cold high-fraction gas S7-V is 75 to 98 volume %.

17. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ The reaction indexes of hydrogenation purification reaction process R2 are as follows: The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 80%; The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 80%; The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 80%; In the hydrogenation purification reaction process R2, the hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon reduces the aromatic carbon ratio by more than 60%; The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 70%; The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%; The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 35 weight %; The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 15 weight %; The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 10 weight %.

18. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ The reaction indexes of hydrogenation purification reaction process R2 are as follows: The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 90%; The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 90%; The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 90%; In the hydrogenation purification reaction process R2, the hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon reduces the aromatic carbon ratio by more than 70%; The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%; The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 90%; The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 17.5 weight %; The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 7.5 weight %; The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 5.0 weight %.

19. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ The reaction indexes of hydrogenation purification reaction process R2 are as follows: The hydrogenation conversion rate of organic oxygen in the raw hydrocarbon to water in the hydrogenation purification reaction process R2 is higher than 98%; The hydrogenation conversion rate of organic nitrogen in the raw hydrocarbon to ammonia in the hydrogenation purification reaction process R2 is higher than 98%; The hydrogenation conversion rate of organic sulfur in the feed hydrocarbon to hydrogen sulfide in the hydrogenation purification reaction process R2 is higher than 98%; The hydrogenation saturation reaction of the overall monocyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 80%; The hydrogenation saturation reaction of the overall bicyclic aromatic hydrocarbons in the feed hydrocarbon of the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 90%; The hydrogenation saturation reaction of the overall polycyclic aromatic hydrocarbons in the feed hydrocarbon in the hydrogenation purification reaction process R2 reduces the aromatic carbon ratio by more than 95%; The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 9 weight %; The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 6 weight %; The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 3 weight %.

20. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ The purification index of hydrogenation purification reaction process R2 is as follows: The weight content of organic oxygen in the hydrocarbons in the hydropurification reaction effluent R2P is less than 5 ppm; The weight content of organic nitrogen in the hydrocarbons in the hydropurification reaction effluent R2P is less than 5 ppm; The organic sulfur content in the hydrocarbons in the hydropurification reaction effluent R2P is less than 2 ppm by weight.

21. The method according to claim 20, characterized in that: ⑶ The purification index of hydrogenation purification reaction process R2 is as follows: The weight content of hydrocarbon components having a normal boiling point higher than 250° C. in the hydropurification reaction effluent R2P is less than 5 weight %; The weight content of hydrocarbon components having a normal boiling point higher than 300° C. in the hydropurification reaction effluent R2P is less than 2 weight %; The weight content of hydrocarbon components having a normal boiling point of more than 350° C. in the hydropurification reaction effluent R2P is less than 1 weight %.

22. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ The operating conditions of the hydrogenation purification reaction process R2 are: pressure of 6-25MPa, temperature of 220-440°C, hydrogen-to-oil ratio of 2000-20000Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.05~10.0h -1 .

23. The method according to claim 22, characterized in that: ⑶ The operating conditions of the hydrogenation purification reaction process R2 are: pressure of 12-20 MPa, temperature of 270-390°C, hydrogen-to-oil ratio of 2000-20000 Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.2~1.0h -1 .

24. The method according to claim 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: The raw hydrocarbons in the hydrocarbon hydrogenation reaction process R1 are hydrocarbon materials containing phenols and aromatics, including hydrocarbons with a conventional boiling point higher than 350°C; The operating conditions of hydrocarbon hydrogenation process R1 are: pressure 6-25MPa, temperature 220-460℃, hydrogen-to-oil ratio 100-3000Nm 3 / t; The operating conditions of the hydrogenation purification reaction process R2 are: pressure of 6-25MPa, temperature of 220-440℃, hydrogen-to-oil ratio of 2000-20000Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.05~10.0h -1 .

25. The method according to claim 24, characterized in that: The raw hydrocarbons in the hydrocarbon hydrogenation reaction process R1 are hydrocarbon materials containing phenols and aromatics, including hydrocarbons with a conventional boiling point higher than 350°C; The operating conditions of hydrocarbon hydrogenation process R1 are: pressure of 12-20 MPa, temperature of 320-440°C, hydrogen-to-oil ratio of 200-2000 Nm 3 / t; ⑶ The operating conditions of the hydrogenation purification reaction process R2 are: pressure of 12-20 MPa, temperature of 270-390°C, hydrogen-to-oil ratio of 2000-20000 Nm 3 / t, the hourly space velocity of hydrogenation purification catalyst liquid is 0.2~1.0h -1 .

26. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; Cold high-purity water S7-W has a phenol content of less than 10ppm and an aromatic content of less than 200ppm.

27. The method according to claim 26, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; Cold high-purity water S7-W has a phenol content of less than 5ppm and an aromatic content of less than 50ppm.

28. The method according to claim 2, characterized in that: (2) In the sewage gasification process U2, at least a part of the vaporizable pollutant components KCM containing water, phenol and / or aromatic hydrocarbons in the first sewage is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V; In the first oil washing process U3, the logistics U2V-1VB based on the first sewage vaporized gas U2V-1 contacts the washing oil U3-AL at least once to obtain the first washed gas U3-PV and the first washed oil U3-PL; The amount of solids in the first washed gas U3-V is less than the amount of solids in the gas phase of the stream U2V-1VB.

29. The method according to claim 28, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; At least a part of the stream based on the cold high fraction oil S7-L is recycled as wash oil U3-AL.

30. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) The gas-containing material R2P-VB based on the hydrogenation purification reaction effluent R2P is mixed with the quenching material KS and cooled to a temperature below the water dew point to form a mixed-phase material R2P-VB-2 containing a gas phase and a liquid phase; The mixed phase material R2P-VB-2 comprises an aqueous phase in which an ammonia component is dissolved.

31. The method according to claim 30, characterized in that: (3) The quenching logistics KS is quenching hydrogen-rich gas and / or quenching oil and / or quenching water.

32. The method according to claim 31, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; The quenching logistics KS is quenching hydrogen-rich gas based on cold high-fraction gas S7-V, and / or quenching oil based on cold high-fraction oil S7-L, and / or quenching water based on cold high-fraction water S7-W.

33. The method according to claim 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) Hydrocarbon hydrogenation reaction process R1, wherein the raw hydrocarbon R1F is a distillation oil obtained by separating the oil generated by the direct liquefaction reaction of coal hydrogenation, the hydrocarbon hydrogenation reaction process R1 undergoes a partial hydrogenation saturation reaction of dicyclic aromatic hydrocarbons and / or polycyclic aromatic hydrocarbons, and the hydrogen supply index of hydrocarbons with a conventional boiling point higher than 200° C. in the reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is higher than the hydrogen supply index of hydrocarbons with a conventional boiling point higher than 200° C. in the raw hydrocarbon R1F; The hydrocarbon oil rich in hydrogen-donating hydrocarbon obtained by separating the hydrogenation reaction effluent R1P is used as a hydrogen-donating solvent and prepared with coal powder to form an oil-coal slurry, which is converted into the coal hydrogenation direct liquefaction reaction effluent through a coal hydrogenation direct liquefaction reaction process; Separating the effluent from the direct liquefaction reaction of coal hydroprocessing to obtain a distillate oil based on the oil produced by the direct liquefaction of coal hydroprocessing, and using it as the feedstock oil R1F of the hydrocarbon hydrogenation reaction process R1; The process of separating the effluent from the direct liquefaction reaction of coal hydroprocessing obtains the initial phenol-containing and aromatic-containing wastewater; Based on the initial phenol-containing and aromatic-containing wastewater, the first wastewater is obtained.

34. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑴The first source of sewage The first sewage, with or without solid particles, is sewage that has undergone a sewage pretreatment process; The sewage pretreatment process includes one or more of the following functions: solid removal, free oil removal, hydrogen sulfide removal, carbon dioxide removal, ammonia removal, and phenol removal.

35. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑴The first sewage is an aqueous solution containing phenol, aromatic hydrocarbons, and chloride ions and / or fluoride ions.

36. The method according to claim 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑵ Wastewater gasification process U2 In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM in the first sewage, including water, phenol and / or aromatic hydrocarbons, is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V; In the cooling and condensing process U203, the first sewage vaporized gas U2V-1 is separated into water-dry gas U203-V and condensed oil U203-L.

37. The method according to claim 36, characterized in that: In the heating process U204, the water-dry gas U203-V absorbs heat and heats up to become the preheated gas U203-V2; The preheated gas U203-V2 enters the hydrogenation purification reaction process R2.

38. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑵ Wastewater gasification process U2 The first sewage vaporization gas U2V-1 is a material containing dust and / or high-boiling-point phenol and / or high-boiling-point aromatic hydrocarbons; In the oil washing liquid process KU52, the gas based on the first sewage vaporization gas U2V-1 contacts with the washing oil KU52-LF at least once to obtain the washed gas KU52-VP and washed oil KU52-LP with lower dust content and / or lower high-boiling phenol content and / or lower high-boiling aromatic hydrocarbon content, and the washed gas enters the hydrogenation purification reaction process R2; At least a part of the wash oil KU52-LF comes from the condensed oil separated in the separation process before the washed gas KU52-VP enters the hydropurification reaction process R2, or comes from the hydrocarbon oil obtained by separating the hydropurification reaction effluent R2P.

39. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the hydrogenation purification reaction process R2, two parallel-operated first branch hydrogenation purification reaction processes R2B1 and second branch hydrogenation purification reaction processes R2B2 are set; When the catalyst operating conditions of the first branch hydrogenation purification reaction process R2B1 are in the final state, most to all of the materials entering the first branch hydrogenation purification reaction process R2B1 are introduced into the second branch hydrogenation purification reaction process R2B2 for hydrogenation purification reaction to extend the continuous operation period.

40. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the hydrogenation purification reaction process R2, two parallel-operated first branch hydrogenation purification reaction processes R2B1 and second branch hydrogenation purification reaction processes R2B2 are set; When the catalyst operating conditions of the first branch hydrogenation purification reaction process R2B1 are in the final state, all materials entering the first branch hydrogenation purification reaction process R2B1 are introduced into the second branch hydrogenation purification reaction process R2B2 for hydrogenation purification reaction, and the first branch hydrogenation purification reaction process R2B1 is isolated from the feed system of the upstream logistics U2V-1B, but hot hydrogen-rich gas is introduced for flow to maintain the operating temperature of the first branch hydrogenation purification reaction process R2B1 within a reasonable range.

41. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the hydrogenation purification reaction process R2, 2 and / or more catalyst beds operated in series are arranged to constitute 2 or more sub-area hydrogenation purification reaction processes operated in series; According to the time course, in the first stage, the logistics U2V-1B passes through the first sub-zone hydrogenation purification reaction process R201, while ensuring that at least hot hydrogen-rich gas flows through the other sub-zones to maintain the operating temperature within a reasonable range; According to the time course, in the second stage, when the catalyst operating conditions of the first sub-area hydrogenation purification reaction process R201 are in the final state, part to all of the logistics U2V-1B entering the first hydrogenation purification reaction process R201 is introduced into the second sub-area hydrogenation purification reaction process R202 for hydrogenation purification reaction, and then it is ensured that at least hot hydrogen-rich gas flows through the first sub-area hydrogenation purification reaction process R201 to maintain the temperature of the first hydrogenation purification reaction process R201 within a reasonable range; When the hydrogenation purification reaction process R2 is provided with 3 or more catalyst beds operated in series, according to the time course, in the third stage, when the catalyst operating conditions of the second sub-area hydrogenation purification reaction process R202 are in the final state, part to all of the logistics U2V-1B entering the second hydrogenation purification reaction process R202 is introduced into the third sub-area hydrogenation purification reaction process R203 for hydrogenation purification reaction, and then it is ensured that at least hot hydrogen-rich gas flows through the second sub-area hydrogenation purification reaction process R202 to maintain the temperature of the second hydrogenation purification reaction process R202 in a reasonable range; By analogy, when the catalyst operating conditions of the last sub-zone hydrogenation purification reaction process R209 are in the final state, a complete operation cycle is completed, and the hydrogenation purification reaction process R2 enters the shutdown step or the first sewage low-load operation step of reducing the first sewage treatment volume.

42. The method according to claim 41, characterized in that: (3) In the hydrogenation purification reaction process R2, when the sub-area hydrogenation purification reaction process R20M processes the flow U2V-1B, the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P without passing through other sub-area hydrogenation purification reaction processes; At the same time, the sub-area hydrogenation purification reaction processes of the other hydrogenation purification reaction processes R2, except the sub-area hydrogenation purification reaction process R20M, neither receive the logistics U2V-1B nor the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M, and only other hot water-poor hydrogen-rich gases flow through; In the reactor of the hydrogenation purification reaction process R2, two or more or all of the sub-area hydrogenation purification reaction processes are arranged in the same pressure equipment shell and the gas phase spaces are interconnected; All sub-areas of the hydrogenation purification reaction process R2 are arranged in one or two or more reactors.

43. The method according to claim 41, characterized in that: (3) In the first stage of the hydrogenation purification reaction process R2, when the first sub-area hydrogenation purification reaction process R201 processes the flow U2V-1B, the reaction product R201P of the first sub-area hydrogenation purification reaction process R201 passes through all other sub-area hydrogenation purification reaction processes located downstream and then is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P; When the sub-area hydrogenation purification reaction process R20M processes the flow U2V-1B, the reaction product R20MP of the sub-area hydrogenation purification reaction process R20M passes through the downstream sub-area hydrogenation purification reaction process and is discharged from the hydrogenation purification reaction process R2 as the hydrogenation purification reaction product R2P; At the same time, all sub-area hydrogenation purification reaction processes located upstream of sub-area hydrogenation purification reaction process R20M do not receive logistics U2V-1B, and only other hot water-poor hydrogen-rich gases flow through, and sub-area hydrogenation purification reaction process R20M receives the effluent from the upstream sub-area hydrogenation purification reaction process; In the reactor of the hydrogenation purification reaction process R2, two or more or all of the sub-area hydrogenation purification reaction processes are arranged in the same pressure equipment shell; All sub-areas of the hydrogenation purification reaction process R2 are arranged in one or two or more reactors.

44. The method according to claim 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) The hydrocarbon feed of the hydrogenation reaction process R1 comprises one or more of the following fractions: ① Hydrocarbons with a conventional boiling point of 200-350°C, including phenols and / or aromatics; ② Hydrocarbons with a conventional boiling point of 350-450°C, including phenols and / or aromatics; ③ Hydrocarbons with a normal boiling point of 450-550°C, including phenols and / or aromatics; The hydrogenation reaction process R1 is a fluidized bed hydrogenation reaction process or a suspended bed hydrogenation reaction process; The reaction effluent R1P of the hydrogenation reaction process R1 is a material containing phenols, aromatic hydrocarbons and water.

45. The method according to claim 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) The hydrocarbon feed of the hydrogenation reaction process R1 is a hydrocarbon stream obtained by separating the product of the direct liquefaction reaction of coal hydrogenation, mainly composed of hydrocarbons with a conventional boiling point of 150 to 550° C., including phenols and aromatics; The hydrogenation reaction process R1 is a fluidized bed hydrogenation reaction process and a suspended bed hydrogenation reaction process; The reaction effluent R1P of the hydrogenation reaction process R1 is a material containing phenols, aromatic hydrocarbons and water.

46. ​​The method according to claim 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (2) The operating temperature of the first sewage vaporized gas U2V-1 obtained in the sewage gasification process U2 is at least 30°C higher than the water dew point; ⑶ The operating temperature of the hydrogenation purification reaction process R2 is at least 50°C higher than the water dew point, and the hydrogen partial pressure of the hydrogenation purification reaction process R2 is 6.0-18.0MPa.

47. The method according to claim 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (2) The operating temperature of the first sewage vaporized gas U2V-1 obtained in the sewage gasification process U2 is at least 30°C higher than the water dew point; ⑶ The operating temperature of the hydrogenation purification reaction process R2 is at least 70°C higher than the water dew point, and the hydrogen partial pressure of the hydrogenation purification reaction process R2 is 9.0-14.0MPa.

48. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the hot high-pressure separation process S1, the reaction effluent R1P of the hydrogenation reaction process R1 is separated to obtain hot high-fraction gas S1-V and hot high-fraction oil S1-L; The hydrocarbon stream S1-L-TOR3 obtained by separating the hot high-fraction oil S1-L enters the hydrogenation purification reaction process R2; The hydrocarbon stream S1-L-TOR3 is mainly composed of hydrocarbons with a conventional boiling point below 250°C and / or hydrocarbons with a boiling point of 250-320°C.

49. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) The clean hydrocarbon stream KEYS containing hydrocarbon components with a conventional boiling point of 300-350°C undergoes a hydrogenation purification reaction process R2, and at least a portion of the clean hydrocarbon stream KEYS remains in a liquid phase during the hydrogenation purification reaction process R2.

50. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; Based on the cold high-pressure separation process feed of the hydrogenation purification reaction effluent R2P, it flows out of the last heat exchanger K-HX for heat recovery to become the logistics K-HX-HP, and the weight flow rate of the liquid water component in the logistics K-HX-HP is not less than 85% of the weight flow rate of the water component in the cold high-pressure water separation S7-W; Logistics K-HX-HP, after being cooled in the cooling process, enters the cold high-pressure separation process S7.

51. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) In the cold high-pressure separation process S7, the hydrogen-containing, water-containing, and hydrocarbon-containing streams based on the hydrogenation purification reaction effluent R2P are separated to obtain cold high-fraction gas S7-V, cold high-fraction water S7-W, and cold high-fraction oil S7-L; Based on the cold high-pressure separation process feed of the hydrogenation purification reaction effluent R2P, it flows out of the last heat exchanger K-HX for heat recovery to become the logistics K-HX-HP, and the temperature of the logistics K-HX-HP is not higher than 150-170℃; Logistics K-HX-HP, after being cooled in the cooling process, enters the cold high-pressure separation process S7.

52. The method of claim 28, wherein: (2) Washing oil U3-AL is a heavy diesel component having a conventional boiling point of 250 to 350°C.

53. The method of claim 38, wherein: (2) Washing oil KU52-LF is a heavy diesel component with a conventional boiling point of 250 to 350°C.

54. The method according to claim 52 or 53, characterized in that: ⑴The first source of sewage The first sewage includes sewage containing phenol, aromatic hydrocarbons and solid particles generated from the separation process of coal hydrogenation direct liquefaction reaction products, and is sewage that has undergone or has not undergone sewage pretreatment; The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process; (2) Washing oil KU52-LF is a heavy diesel component with a conventional boiling point of 250-350°C. It is heavy diesel DIES100 distilled from the oil generated by the hydrogenation and modification reaction of "coal hydrogenation direct liquefaction oil and / or hydrogenation and modification oil of coal hydrogenation direct liquefaction oil", or it is the rich absorption oil formed by the heavy diesel DIES100 through the recovery of liquefied gas and gasoline absorption process of gas containing liquefied gas and light gasoline components. In this way, heavy diesel DIES100 can be used in series twice.

55. The method according to claim 52 or 53, characterized in that: ⑴The first source of sewage The first sewage includes sewage containing phenol, aromatic hydrocarbons and solid particles generated from the separation process of coal hydrogenation direct liquefaction reaction products, and is sewage that has undergone or has not undergone sewage pretreatment; The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process; (2) Washing oil KU52-LF is a heavy diesel component with a conventional boiling point of 250-350°C. It is heavy diesel DIES100 distilled from the oil generated by the hydrogenation and modification reaction of "coal hydrogenation direct liquefaction oil and / or hydrogenation and modification oil of coal hydrogenation direct liquefaction oil", or it is the rich absorption oil formed by the heavy diesel DIES100 through the recovery of liquefied gas and gasoline absorption process of gas containing liquefied gas and light gasoline components. In this way, heavy diesel DIES100 can be used in series twice.

56. The method according to claim 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑴The first source of sewage The first sewage, containing or not containing solid particles, is the sewage of the initial sewage with or without the sewage pretreatment process; The sewage pretreatment process includes one or more of the following functions: a solid removal process before the hydrogen sulfide and deamination process, a free oil removal process, a hydrogen sulfide and carbon dioxide removal process, a deamination process, and a phenol removal process; ⑵ Wastewater gasification process U2 In the first sewage light oil desolidification process, the first sewage is mixed with the first desolidified hydrocarbon oil feedstock and separated into the first desolidified oil-rich sewage and the first solid-reduced sewage; The solid content in the first desolidified rich oil is higher than the solid content in the first desolidified hydrocarbon oil feedstock; The solid content in the first solids-reducing sewage is lower than the solid content in the first sewage; In the sewage gasification process U2, at least a portion of the vaporizable pollutant components KCM including water, phenol and / or aromatic hydrocarbons in the first solid reduction sewage is vaporized into a vaporized gas KCM-V, and a first sewage vaporized gas U2V-1 is obtained based on the vaporized gas KCM-V; The first sewage vaporized gas U2V-1 is water-wet gas or water-dry gas; The first sewage vaporized gas U2V-1 may contain or may not contain liquid hydrocarbon oil.

57. The method according to claim 56, characterized in that: (2) In the first sewage light oil desolidification process, the first desolidified hydrocarbon oil raw material is a hydrocarbon oil based on the condensed oil of the sewage gasification process U2, and / or is a hydrocarbon oil obtained by separating the hydrogenation purification reaction effluent R2P; The first solids are removed and the oil is enriched, and then the solids are washed with oil before entering the solids removal process before the hydrogen sulfide removal and deammoniation process; In the pre-solids removal process before the dehydrogensulfurization and deammoniation process, the first desolids-rich oil-rich logistics is mixed and contacted with the pre-wastewater logistics based on the initial wastewater to separate into pre-solids-rich oil-rich and pre-solids-reduced wastewater; The solid content in the pre-solidification rich oil is higher than the solid content in the first desolidification rich oil; The solid content in the front solids reduction sewage is lower than the solid content in the front sewage stream; Based on the logistics of the pre-solid reduction sewage, it goes through the first sewage light oil desolidification process.

58. The method according to claim 57, characterized in that: (3) The reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1; the hot high-fraction oil R1P-S1L contains solid particles; The logistics based on the hot high-fraction gas R1P-S1V is mixed and contacted with the logistics based on the first sewage to form a water-dry or water-wet first sewage vaporized gas U2V-1; In the separation and fractionation process FRAC80, the hot high fraction oil R1P-S1L is separated into gas, narrow fraction oil products, and separation bottom oil FRAC80-DV containing solid particles; The oil-rich logistics based on the pre-solid removal enters the separation and fractionation process FRAC80 and is mixed with the logistics based on the thermal high oil separation R1P-S1L to separate into narrow-fraction oil products. The solid particles contained in the oil-rich logistics based on the pre-solid removal enter the separation bottom oil FRAC80-DV.

59. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ In the hydrogenation purification reaction process R2, other hydrocarbons P600 mainly containing phenols and / or aromatic bodies with a conventional boiling point below 350°C are processed together; Hydrocarbons P600, including or not including the hydrocarbon stream obtained by separating the oil produced by direct liquefaction of coal.

60. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ In the hydrogenation purification reaction process R2, other hydrocarbons P700 mainly containing phenols and / or aromatic bodies with a conventional boiling point below 250°C are processed together; Hydrocarbons P700, including or not including the hydrocarbon stream obtained by separating the oil produced by direct liquefaction of coal.

61. The method according to claim 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: (3) The reaction effluent R1P of the hydrocarbon hydrogenation reaction process R1 is separated into hot high-fraction gas R1P-S1V and hot high-fraction oil R1P-S1L in the hot high-pressure separation process R1P-S1; The hot high-fraction oil R1P-S1L is separated and mainly contains phenol and / or aromatic hydrocarbons with a conventional boiling point below 250°C, which enter the hydrogenation purification reaction process R2 for joint processing.

62. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑴ The first source of wastewater is wastewater with low chloride ion content, which is selected from the top water of the distillation tower and vacuum tower of coal hydrogenation direct liquefaction oil, the top water of the distillation tower of the hydrogenation modification oil generated by coal hydrogenation direct liquefaction, and gas fractionation acidic water.

63. The method according to claim 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑶ Hydrocarbon hydrogenation reaction process R1 is a hydrogenation and upgrading reaction process of coal direct liquefaction oil or hydrogenated modified oil of coal direct liquefaction oil.

64. The method according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11, characterized in that: ⑵ Wastewater gasification process U2 The first sewage vaporized gas U2V-1 is a material containing dust and / or high-boiling-point phenols and / or high-boiling-point aromatic hydrocarbons. The gas based on the first sewage vaporized gas U2V-1 undergoes a cooling, condensation, separation and deliquescence process KU51 and / or an oil eluent process KU52 to obtain a gas with a lower dust content and / or a lower high-boiling-point phenol content and / or a lower high-boiling-point aromatic hydrocarbon content and enters the hydrogenation purification reaction process R2.

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