Method for separating hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide

Abstract

The separation method of the hydrocarbon hydrogenation product containing ammonia, hydrogen chloride and / or hydrogen sulfide is particularly suitable for the condition that the flow rate of ammonia and / or the flow rate of water and gas is large in the hydrocarbon hydrogenation product, and can greatly reduce the amount of external washing water, greatly reduce the yield of acidic water, improve the heat recovery rate and reduce the content of organic matters in cold high-pressure separated water. The method is suitable for separation of warm high-pressure separated gas separated from hot high-pressure separated gas of coal hydrogenation direct liquefaction reaction effluent, the warm high-pressure separated gas is mixed with circulating auxiliary-temperature high-pressure separated water to form a mixture M-100 which is higher in water dew point temperature and has a large amount of liquid-water phase, and auxiliary-temperature high-pressure separated gas, auxiliary-temperature high-pressure separated oil and auxiliary-temperature high-pressure separated water are separated in the auxiliary-temperature high-pressure separation process through heat release of a heat exchanger HX-K; the secondary temperature high-pressure separation water is divided into two paths, one path is used as circulating secondary temperature high-pressure separation water, and the other path is used as a secondary temperature high-pressure separation water clean product which is usually mixed with secondary temperature high-pressure separation gas to form a mixed material M-500, and cold high-pressure separation water, cold high-pressure separation oil and cold high-pressure separation gas are separated in the cold high-pressure separation process after heat exchange and heat dissipation.

Description

Technical Field

[0001] The present invention relates to a process for separating hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide. Background Art

[0002] The present invention discloses a method for separating hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide. The method is particularly suitable for the situation that the ammonia flow rate and / or water gas volume in the hydrocarbon hydrogenation products are large and the hydrogen flow rate is large. The method can greatly reduce the amount of external washing water and the production of acidic water. The method is suitable for separating the hot high-fraction gas separated from the effluent of the direct liquefaction reaction of coal hydrogenation, and mixing the hot high-fraction gas with the circulating secondary temperature high-fraction water to form a mixture M-100 with a higher water dew point temperature and a large amount of liquid-water phase, and then releasing heat through the heat exchanger HX-K to enter the secondary temperature high-pressure separation process. The process separates the secondary temperature high fraction gas, secondary temperature high fraction oil and secondary temperature high fraction water; the secondary temperature high fraction water is divided into two paths, one is used as the circulating secondary temperature high fraction water, and the other is used as the secondary temperature high fraction water. The net product is usually mixed with the secondary temperature high fraction gas to form a mixed material M-500. After heat exchange and heat dissipation, cold high fraction water, cold high fraction oil and cold high fraction gas are separated in the cold high pressure separation process; under the condition of avoiding the corrosion of high concentration chloride ion water mist, the amount of external water injection can be reduced, the output of cold high fraction water can be reduced, the number of hydrocarbons and the carbon number of hydrocarbons in cold high fraction water can be reduced, and the area of ​​heat exchanger HX-K can be reduced.

[0003] Compared with the conventional separation method of hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide, the separation method of hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide of the present invention is essentially a method of using the phase equilibrium principle to change the total amount of water components in the material by circulating sub-temperature high water separation, thereby increasing the water dew point temperature of the mixture M-100, and achieving one or more of the following main goals under the condition of avoiding the corrosion of high-concentration chloride ion water mist:

[0004] ① The hot high-fraction gas separated from the hot high-fraction gas of the direct liquefaction reaction of coal hydrogenation or the hot high-fraction gas separated from the effluent of the solvent oil hydrogenation stabilization reaction supporting the direct liquefaction of coal hydrogenation is mixed with the circulating sub-temperature high-fraction water to form a mixture M-100 with a large amount of liquid-water phase, avoiding the strong corrosion conditions of high-concentration chloride ion water mist in the area near the water dew point that will inevitably occur if water is not injected. The presence of a large amount of liquid phase water forms low-concentration chloride ion liquid phase water;

[0005] The flushing water volume can be adjusted flexibly without increasing the amount of acidic water net products;

[0006] ② Reducing the amount of external water injection increases the concentration of pollutants in acidic water, which can reduce the total output of acidic sewage and reduce the scale, investment and energy consumption of the subsequent treatment system (including heat exchange and heat dissipation system) of acidic sewage;

[0007] ③ Since the circulation path of the circulating secondary temperature high separation water does not involve a cooling radiator (such as an air cooler or a water cooler), all of them are heat exchangers for recovering medium temperature heat, so the medium temperature heat absorbed by the circulating secondary temperature high separation water as a heat energy carrier from the warm high separation gas NO1 is theoretically not lost;

[0008] ④ Reduce the amount of external water injection, reduce the total output of acidic sewage, and reduce the low-temperature heat from the high-temperature fraction NO1 released by the external water injection material as a heat carrier through the radiator (such as air cooler, water cooler), which can improve the low-temperature heat recovery rate and reduce the load of the radiator (such as air cooler, water cooler), that is, reduce the investment in the radiator (such as air cooler, water cooler);

[0009] ⑤ Increasing the water dew point temperature of the mixture M-100, that is, increasing the temperature of the mixture M-100, can increase the heat transfer temperature difference of the heat exchanger HX-K of the mixture M-100, that is, reduce the area of ​​the heat exchanger HX-K;

[0010] ⑥ The secondary temperature high pressure separation process produces secondary temperature high fraction oil, thereby reducing the content of high boiling point hydrocarbon components in the cold high fraction oil, which is beneficial to reduce the distillation dry point of dissolved hydrocarbons in the cold high fraction water, reduce the deoiling task of the subsequent purification process of the cold high fraction water, and reduce the digestion load of the biochemical process;

[0011] ⑦ Keep the net product temperature of the secondary temperature high oil separation, improve the low-temperature heat recovery rate, reduce the load of the radiator (such as air cooler, water cooler), that is, reduce the investment in the radiator (such as air cooler, water cooler);

[0012] ⑧ For hydrocarbon hydrogenation products containing a large amount of ammonia and hydrogen chloride, an intermittent water injection flushing scheme is conventionally adopted to prevent ammonium chloride from clogging the flow channel due to deposition. This scheme will cause chloride salt corrosion on the surface of the metal material where the solid is deposited. The present invention provides a method for continuous flushing of ammonium chloride with a simple process, low investment, and no consumption of external special ammonium chloride flushing water, and at the same time has multiple beneficial functions.

[0013] The present invention is suitable for newly-built devices or for the transformation of existing devices.

[0014] The method of the present invention has not been reported.

[0015] A first object of the present invention is to provide a method for separating hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide.

[0016] The second object of the present invention is to provide a method for increasing the water dew point temperature of hydrocarbon hydrogenation products containing water, hydrogen chloride and ammonia.

[0017] The third object of the present invention is to provide a method for reducing the amount of external washing water used for hydrocarbon hydrogenation products containing water, hydrogen chloride and ammonia and reducing the production of acidic water.

[0018] A fourth object of the present invention is to provide a method for improving the medium-temperature heat recovery rate in the area near the water dew point of hydrocarbon hydrogenation products containing water, hydrogen chloride and ammonia.

[0019] A fifth object of the present invention is to provide a method for reducing the area of ​​a heat recovery heat exchanger for recovering medium-temperature heat energy in the vicinity of the water dew point of a hydrocarbon hydrogenation product containing water, hydrogen chloride, and ammonia.

[0020] The sixth object of the present invention is to provide a method for reducing the area of ​​the heat dissipation heat exchanger in the temperature region below the water dew point for recovering hydrocarbon hydrogenation products containing water, hydrogen chloride and ammonia.

[0021] The seventh object of the present invention is to provide a method for economical continuous water injection flushing of hydrocarbon hydrogenation products in the presence of large amounts of ammonia and hydrogen chloride. Summary of the invention

[0022] The method for separating hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide of the present invention is characterized by comprising the following steps:

[0023] The hydrogenation reaction effluent R1P produced by the hydrocarbon material hydrogenation reaction process R1 is a gas-liquid mixed phase material containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide;

[0024] The gas phase of the hydrogenation reaction effluent R1P is a gas phase containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide, with or without water vapor;

[0025] In the flash separation process of the hydrogenation reaction effluent R1P, a base gas containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide is separated;

[0026] The gas phase-containing material N-01 obtained based on the base gas is a gas phase-containing material containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide, with or without water vapor;

[0027] Logistics N-01 is mixed with circulating secondary temperature high-divided water to form a mixture M-100 with a higher water dew point temperature and a large amount of liquid water phase;

[0028] The mixture M-100 is cooled by heat exchanger HX-K and enters the secondary temperature high pressure separation process to separate secondary temperature high separation gas, secondary temperature high separation oil and secondary temperature high separation water;

[0029] The logistics of secondary temperature high separation water is divided into two routes, one is used as the basic material of secondary temperature high separation water circulation, and the other is used as the net product of secondary temperature high separation water;

[0030] The aqueous stream based on the circulating sub-temperature high separation water base material is used as circulating sub-temperature high separation water.

[0031] In the present invention, usually, the logistics based on the sub-temperature high-separation water net product and the logistics based on the sub-temperature high-separation gas are mixed into a mixed material M-500, and the mixed material M-500 enters a cold high-pressure separation process after being cooled to separate cold high-separation water, cold high-separation oil, and cold high-separation gas.

[0032] In the present invention, the hydrocarbon material processed in the hydrocarbon material hydrogenation reaction process R1 can be selected from one or more of the following materials:

[0033] ① Low-temperature coal tar or its fractions or oil products obtained by thermal processing, the thermal processing process is coking process or catalytic cracking process or catalytic cracking process;

[0034] ② Medium-temperature coal tar or its fractions or oil products obtained from its thermal processing;

[0035] ③ High-temperature coal tar or its fractions or oil products obtained from its thermal processing;

[0036] ④ Oil-coal slurry used in the process of direct liquefaction of coal by hydrogenation;

[0037] ⑤ Oil products obtained from the coal hydrogenation direct liquefaction oil production process, the coal hydrogenation direct liquefaction oil production process is selected from one or more of the coal hydrogenation direct liquefaction oil production process without using hydrogen-donating solvent oil, the coal hydrogenation direct liquefaction oil production process using hydrogen-donating solvent oil, the oil-coal co-refining process, and the coal hydrogenation thermal solution process;

[0038] ⑥ Petroleum-based heavy oil or its fractions or oil products obtained through thermal processing;

[0039] 7. Shale oil or its fractions or oil products obtained through thermal processing;

[0040] ⑧ Petroleum sand-based heavy oil or its fractions or oil products obtained through thermal processing;

[0041] ⑨Other hydrocarbon oils with a resin content higher than 15% by weight and / or an asphaltene content higher than 5.0% by weight.

[0042] In the present invention, the hydrocarbon material hydrogenation reaction process R1 can be selected from one of the following processes:

[0043] ① Direct liquefaction of coal by hydrogenation to produce oil;

[0044] ② The hydrogenation process of coal hydrogenation direct liquefaction oil;

[0045] ③Coal tar hydrogenation process;

[0046] ④ Hydrogenation process of petroleum-based heavy oil;

[0047] ⑤Hydrogenation process of shale oil;

[0048] ⑥Hydrogenation process of petroleum sand-based oil.

[0049] In the present invention, generally, the operating conditions of the hydrocarbon material hydrogenation reaction process R1 are: pressure of 6 to 25 MPa and temperature of 220 to 460°C;

[0050] The weight flow rate of the circulating sub-temperature high-separation water is 0.3 to 10 times the weight flow rate of the net product of the sub-temperature high-separation water.

[0051] In the present invention, logistics N-01 can be selected from one of the following:

[0052] ① The hydrogenation reaction effluent R1P is separated into hot high-fraction gas and hot high-fraction oil in the hot high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 220-460℃;

[0053] The hot high-fraction gas is used as logistics N-01;

[0054] ② The hydrogenation reaction effluent R1P is separated into hot high-fraction gas and hot high-fraction oil in a hot high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 220-460℃;

[0055] The hot high-fraction gas is separated into hot high-fraction gas and hot high-fraction oil in the hot and high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 250-350℃;

[0056] The warm high-pressure gas is used as logistics N-01.

[0057] In the present invention, generally, the weight concentration of chloride ions in the auxiliary temperature high separation water can be selected from one of the following:

[0058] ①1000~500ppm; ②500~300ppm; ③300~200ppm; ④200~150ppm; ⑤<150ppm.

[0059] In the present invention, generally, the operating temperature of the mixture M-100 is at least 10°C below its water dew point temperature.

[0060] In the present invention, usually, the operating temperature of the secondary temperature high pressure separation process is 180-280°C.

[0061] In the present invention, before logistics N-09 based on logistics N-01 enters the cold high-pressure separation process, no other washing water logistics are added except for the circulating sub-temperature high-separation water. DETAILED DESCRIPTION

[0062] The present invention is described in detail below.

[0063] The pressure described in the present invention is equivalent to the standard physical term pressure.

[0064] The conventional boiling point described in the present invention refers to the vapor-liquid equilibrium temperature of a substance at one atmospheric pressure.

[0065] The conventional boiling point range described in the present invention refers to the conventional boiling point range of the distillate.

[0066] The composition, concentration, content or yield of the components described in the present invention are all weight-based values ​​unless otherwise specified.

[0067] The characteristic parts of the present invention are described below.

[0068] The method for separating hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide of the present invention is characterized by comprising the following steps:

[0069] The hydrogenation reaction effluent R1P produced by the hydrocarbon material hydrogenation reaction process R1 is a gas-liquid mixed phase material containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide;

[0070] The gas phase of the hydrogenation reaction effluent R1P is a gas phase containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide, with or without water vapor;

[0071] In the flash separation process of the hydrogenation reaction effluent R1P, a base gas containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide is separated;

[0072] The gas phase-containing material N-01 obtained based on the base gas is a gas phase-containing material containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide, with or without water vapor;

[0073] Logistics N-01 is mixed with circulating secondary temperature high-divided water to form a mixture M-100 with a higher water dew point temperature and a large amount of liquid water phase;

[0074] The mixture M-100 is cooled by heat exchanger HX-K and enters the secondary temperature high pressure separation process to separate secondary temperature high separation gas, secondary temperature high separation oil and secondary temperature high separation water;

[0075] The logistics of secondary temperature high separation water is divided into two routes, one is used as the basic material of secondary temperature high separation water circulation, and the other is used as the net product of secondary temperature high separation water;

[0076] The aqueous stream based on the circulating sub-temperature high separation water base material is used as circulating sub-temperature high separation water.

[0077] In the present invention, usually, the logistics based on the sub-temperature high-separation water net product and the logistics based on the sub-temperature high-separation gas are mixed into a mixed material M-500, and the mixed material M-500 enters a cold high-pressure separation process after being cooled to separate cold high-separation water, cold high-separation oil, and cold high-separation gas.

[0078] In the present invention, the hydrocarbon material processed in the hydrocarbon material hydrogenation reaction process R1 can be selected from one or more of the following materials:

[0079] ① Low-temperature coal tar or its fractions or oil products obtained by thermal processing, the thermal processing process is coking process or catalytic cracking process or catalytic cracking process;

[0080] ② Medium-temperature coal tar or its fractions or oil products obtained from its thermal processing;

[0081] ③ High-temperature coal tar or its fractions or oil products obtained from its thermal processing;

[0082] ④ Oil-coal slurry used in the process of direct liquefaction of coal by hydrogenation;

[0083] ⑤ Oil products obtained from the coal hydrogenation direct liquefaction oil production process, the coal hydrogenation direct liquefaction oil production process is selected from one or more of the coal hydrogenation direct liquefaction oil production process without using hydrogen-donating solvent oil, the coal hydrogenation direct liquefaction oil production process using hydrogen-donating solvent oil, the oil-coal co-refining process, and the coal hydrogenation thermal solution process;

[0084] ⑥ Petroleum-based heavy oil or its fractions or oil products obtained through thermal processing;

[0085] 7. Shale oil or its fractions or oil products obtained through thermal processing;

[0086] ⑧ Petroleum sand-based heavy oil or its fractions or oil products obtained through thermal processing;

[0087] ⑨Other hydrocarbon oils with a resin content higher than 15% by weight and / or an asphaltene content higher than 5.0% by weight.

[0088] In the present invention, the hydrocarbon material hydrogenation reaction process R1 can be selected from one of the following processes:

[0089] ① Direct liquefaction of coal by hydrogenation to produce oil;

[0090] ② The hydrogenation process of coal hydrogenation direct liquefaction oil;

[0091] ③Coal tar hydrogenation process;

[0092] ④ Hydrogenation process of petroleum-based heavy oil;

[0093] ⑤Hydrogenation process of shale oil;

[0094] ⑥Hydrogenation process of petroleum sand-based oil.

[0095] In the present invention, generally, the operating conditions of the hydrocarbon material hydrogenation reaction process R1 are: pressure of 6 to 25 MPa and temperature of 220 to 460°C;

[0096] The weight flow rate of the circulating sub-temperature high-separation water is 0.3 to 10 times the weight flow rate of the net product of the sub-temperature high-separation water.

[0097] In the present invention, logistics N-01 can be selected from one of the following:

[0098] ① The hydrogenation reaction effluent R1P is separated into hot high-fraction gas and hot high-fraction oil in the hot high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 220-460℃;

[0099] The hot high-fraction gas is used as logistics N-01;

[0100] ② The hydrogenation reaction effluent R1P is separated into hot high-fraction gas and hot high-fraction oil in a hot high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 220-460℃;

[0101] The hot high-fraction gas is separated into hot high-fraction gas and hot high-fraction oil in the hot and high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 250-350℃;

[0102] The warm high-pressure gas is used as logistics N-01.

[0103] In the present invention, generally, the weight concentration of chloride ions in the auxiliary temperature high separation water can be selected from one of the following:

[0104] ①1000~500ppm; ②500~300ppm; ③300~200ppm; ④200~150ppm; ⑤<150ppm.

[0105] In the present invention, generally, the operating temperature of the mixture M-100 is at least 10°C below its water dew point temperature.

[0106] In the present invention, usually, the operating temperature of the secondary temperature high pressure separation process is 180-280°C.

[0107] In the present invention, before logistics N-09 based on logistics N-01 enters the cold high-pressure separation process, no other washing water logistics are added except for the circulating sub-temperature high-separation water.

[0108] Example

[0109] Comparative Example 1

[0110] The hot high-pressure separator of a hydrogenation reaction effluent separates a hot high-fraction gas with a pressure of 18.65MPa and a temperature of 420℃. The hot high-fraction gas is separated in the warm high-pressure separator into a warm high-fraction gas N01 (water dew point 221.87℃) with a pressure of 18.185MPa and a temperature of 285℃.

[0111] The composition of warm high-gas NO1 is shown in Table 1, containing 2.415 kg / h of hydrogen chloride HCL. The crystallization and deposition temperature of NH4CL in warm high-gas NO1 is about 238°C.

[0112] In order to prevent the occurrence of strong corrosive conditions of high-concentration chloride ion water mist, the area near the water dew point temperature needs to be cooled quickly and a large amount of liquid water needs to be formed to absorb chloride ions and form a liquid-phase aqueous solution with a low chloride ion concentration. According to the conventional water injection plan, 25 t / h of 40°C flushing water needs to be injected. The operating conditions of the mixture NO2 (water dew point 247.75°C) after water injection are: pressure 18.485 MPa, temperature 235.92°C, and the phase equilibrium calculation results show that the free water phase contains 13.210 t / h of water; after water injection, the logistics enters a cold high-pressure separator with a pressure of 18.185 MPa and a temperature of 54°C to separate a cold high-fraction water phase containing 59.082 t / h of water, and the weight flow rate of chloride ions converted to HCL is 2.415 kg / h.

[0113] Example 1

[0114] According to the improved comparative example 1 of the method of the present invention, a secondary temperature high pressure separator is set to separate the secondary temperature high separation water, and the circulating secondary temperature high separation water with a temperature of 200°C and a flow rate of 55.000t / h is injected into the warm high separation gas NO1 to form a mixture M-100 with a pressure of 18.485MPa and a temperature of 240.23°C (the water dew point temperature is 266.87°C, which is about 19°C higher than the water dew point of the mixture NO2 of 247.75°C). The mixture M-100 is cooled to 200°C and enters the secondary temperature high pressure separator to be separated into secondary temperature high pressure separation gas, secondary temperature high pressure separation water, and secondary temperature high pressure separation oil. The phase equilibrium calculation results of the secondary temperature high pressure separator are shown in Table 1 ; The secondary temperature high pressure separation water is divided into two routes: circulating secondary temperature high pressure separation water and secondary temperature high pressure separation water net product; the mixture of secondary temperature high pressure separation gas and secondary temperature high pressure separation water net product M-500 is cooled and enters the cold high pressure separator with a pressure of 18.185MPa and a temperature of 54℃. The output of cold high pressure separation water is 32.757t / h, and the weight flow rate of chloride ions converted to HCL is 2.415kg / h. The amount of acidic water net product is reduced by 26.325t / h, which reduces the processing load of the subsequent purification processes of acidic water such as deoiling, filtration, extraction, dehydrogen sulfide removal, deammoniation and dephenolization by about 26.325t / h.

[0115] Table 1 shows the flushing scheme of warm high-pressure gas NO1 and the logistics data of the secondary temperature high-pressure separator.

[0116] Table 2 is the flash phase equilibrium data of warm and high-pressure gas NO1.

[0117] Table 3 is the flash phase equilibrium data of mixture NO2.

[0118] Table 4 shows the flash phase equilibrium data of mixture M-100.

[0119] Table 5 is a comparison table of distillation curves of sub-temperature high-fraction oil and cold high-fraction oil.

[0120] Compared with the conventional method, this embodiment shows the following advantages:

[0121] ① 2.2 times the flushing water volume can be used, while reducing the amount of acidic water net product by 26.325t / h;

[0122] ② Reduce the external water injection volume by 25t / h, increase the concentration of pollutants in acidic water, reduce the total output of acidic sewage, and reduce the scale, investment and energy consumption of the subsequent treatment system of acidic sewage (including the heat exchange and heat dissipation system of the mixed material M-500);

[0123] ③ Since the circulation path of the circulating secondary temperature high separation water does not involve a radiator (such as an air cooler or a water cooler), all of them are heat exchangers for recovering medium temperature heat, the circulating secondary temperature high separation water, as a heat energy carrier, absorbs medium temperature heat from the high temperature high separation gas NO1.

[0124] In theory, there is no loss;

[0125] ④ Reduce the external water injection volume by 25t / h, reduce the total output of acidic sewage, and reduce the external water injection material as a heat carrier through the radiator (such as air cooler, water cooler). The low-temperature heat (about 4200KW) released from the high-temperature fraction NO1 from 200℃ to 54℃ can improve the low-temperature heat recovery rate and reduce the load of the radiator (such as air cooler, water cooler), that is, reduce the investment in the radiator (such as air cooler, water cooler);

[0126] ⑤ The water dew point temperature of the mixture M-100 is increased by about 19°C, that is, the temperature of the mixture M-100 is increased, which can increase the heat transfer temperature difference of the heat exchanger HX-K of the mixture M-100, and can reduce the area of ​​the heat exchanger HX-K;

[0127] ⑥ The secondary temperature high pressure separation process produces secondary temperature high separation oil net product, thereby reducing the content of high boiling point hydrocarbon components in cold high separation oil, which is beneficial to reduce the distillation dry point of hydrocarbons dissolved in cold high separation water, reduce the deoiling task of the subsequent purification process of cold high separation water, and reduce the digestion load of the biochemical process;

[0128] As can be seen from Table 5, the temperature of the distillation point from 30 wt% to 99 wt% of the TBP temperature of 760 mm HG of the cold high fraction oil is at least 59°C lower than the temperature of the corresponding distillation point from 30 wt% to 99 wt% of the TBP temperature of 760 mm HG of the secondary temperature high fraction oil;

[0129] ⑦ Maintain the temperature of the sub-temperature high-separation oil S5L net product, reduce the pressure and degassing before entering the distillation tower, thereby improving the low-temperature heat recovery rate, reducing the load of the radiator (such as air cooler, water cooler), and reducing the investment in the radiator (such as air cooler, water cooler).

[0130] Table 1 Flushing scheme of warm high-pressure gas NO1 and logistics data of sub-temperature high-pressure separator

[0131]

[0132]

[0133] Table 2 Flash phase equilibrium data of warm and high-pressure gas NO1

[0134]

[0135] Table 3 Flash phase equilibrium data of mixture NO2

[0136]

[0137]

[0138] Table 4 Flash phase equilibrium data of mixture M-100

[0139]

[0140] Table 5 Comparison of distillation curves of sub-temperature high-fraction oil and cold high-fraction oil

[0141]

Claims

1. A method for separating hydrocarbon hydrogenation products containing ammonia, hydrogen chloride and / or hydrogen sulfide, characterized in that The following steps are involved: The hydrogenation reaction effluent R1P produced by the hydrocarbon material hydrogenation reaction process R1 is a gas-liquid mixed phase material containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide; The gas phase of the hydrogenation reaction effluent R1P is a gas phase containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide, with or without water vapor; In the flash separation process of the hydrogenation reaction effluent R1P, a base gas containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide is separated; The gas phase-containing material N-01 obtained based on the base gas is a gas phase-containing material containing hydrogen, conventional liquid hydrocarbons, ammonia, hydrogen chloride and / or hydrogen sulfide, with or without water vapor; Logistics N-01 is mixed with circulating secondary temperature high-divided water to form a mixture M-100 with a higher water dew point temperature and a large amount of liquid water phase; The mixture M-100 is cooled by heat exchanger HX-K and then enters the secondary temperature high pressure separation process to separate secondary temperature high separation gas, secondary temperature high separation oil and secondary temperature high separation water; The logistics of secondary temperature high separation water is divided into two routes, one is used as the basic material of secondary temperature high separation water circulation, and the other is used as the net product of secondary temperature high separation water; The aqueous stream based on the circulating sub-temperature high separation water base material is used as circulating sub-temperature high separation water.

2. The method according to claim 1, characterized in that: The logistics of the net product based on the secondary temperature high fraction water and the logistics based on the secondary temperature high fraction gas are mixed into the mixed material M-500. After cooling, the mixed material M-500 enters the cold high pressure separation process to separate the cold high fraction water, cold high fraction oil and cold high fraction gas.

3. The method according to claim 1, characterized in that: The hydrocarbon material processed in the hydrocarbon material hydrogenation reaction process R1 is selected from one or more of the following materials: ① Low-temperature coal tar or its fractions or oil products obtained by thermal processing, the thermal processing process is coking process or catalytic cracking process or catalytic cracking process; ② Medium-temperature coal tar or its fractions or oil products obtained from its thermal processing; ③ High-temperature coal tar or its fractions or oil products obtained from its thermal processing; ④ Oil-coal slurry used in the process of direct liquefaction of coal by hydrogenation; ⑤ Oil products obtained from the coal hydrogenation direct liquefaction oil production process, the coal hydrogenation direct liquefaction oil production process is selected from one or more of the coal hydrogenation direct liquefaction oil production process without using hydrogen-donating solvent oil, the coal hydrogenation direct liquefaction oil production process using hydrogen-donating solvent oil, the oil-coal co-refining process, and the coal hydrogenation thermal solution process; ⑥ Petroleum-based heavy oil or its fractions or oil products obtained through thermal processing; 7. Shale oil or its fractions or oil products obtained through thermal processing; ⑧ Petroleum sand-based heavy oil or its fractions or oil products obtained from thermal processing; ⑨Other hydrocarbon oils with a resin content higher than 15% by weight and / or an asphaltene content higher than 5.0% by weight.

4. The method according to claim 1, characterized in that: The hydrocarbon material hydrogenation reaction process R1 is selected from one of the following processes: ① Direct coal liquefaction process; ② The hydrogenation process of coal hydrogenation direct liquefaction oil; ③Coal tar hydrogenation process; ④ Hydrogenation process of petroleum-based heavy oil; ⑤Shale oil hydrogenation process; ⑥Hydrogenation process of petroleum sand-based oil.

5. The method according to claim 1, 2, 3 or 4, characterized in that: The operating conditions of hydrocarbon material hydrogenation reaction process R1 are: pressure of 6-25MPa and temperature of 220-460°C; The weight flow rate of the circulating sub-temperature high-separation water is 0.3 to 10 times the weight flow rate of the net product of the sub-temperature high-separation water.

6. The method according to claim 1 or 2 or 3 or 4, characterized in that: Logistics N-01, selected from one of the following: ① The hydrogenation reaction effluent R1P is separated into hot high-fraction gas and hot high-fraction oil in the hot high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 220-460℃; The hot high-fraction gas is used as logistics N-01; ② The hydrogenation reaction effluent R1P is separated into hot high-fraction gas and hot high-fraction oil in a hot high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 220-460℃; The hot high-fraction gas is separated into hot high-fraction gas and hot high-fraction oil in the hot and high-pressure separation process. The operating conditions are: pressure of 6-25MPa and temperature of 250-350℃; The warm high-pressure gas is used as logistics N-01.

7. The method according to claim 1 or 2 or 3 or 4, characterized in that: The weight concentration of chloride ions in the sub-temperature high-density water is selected from one of the following: ①1000~500ppm; ②500~300ppm; ③300~200ppm; ④200~150ppm; ⑤<150ppm.

8. The method according to claim 1 or 2 or 3 or 4, characterized in that: The operating temperature of the mixture M-100 is at least 10°C below its water dew point.

9. The method according to claim 1 or 2 or 3 or 4, characterized in that: The operating temperature of the secondary temperature high pressure separation process is 180-280°C.

10. The method according to claim 2, 3 or 4, characterized in that: Before logistics N-09 based on logistics N-01 enters the cold high-pressure separation process, no other washing water logistics are added except for the circulating sub-temperature high-separation water.

Images