CN103482581A - Method for co-producing sulfur and hydrofined product - Google Patents
Method for co-producing sulfur and hydrofined product Download PDFInfo
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- CN103482581A CN103482581A CN201210193073.8A CN201210193073A CN103482581A CN 103482581 A CN103482581 A CN 103482581A CN 201210193073 A CN201210193073 A CN 201210193073A CN 103482581 A CN103482581 A CN 103482581A
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Abstract
The invention discloses a method for co-producing sulfur and a hydrofined product. The method comprises sequentially or simultaneously carrying out the following steps: (1) under a Claus reaction condition, contacting acid gas containing hydrogen sulfide with oxygen-containing-gas, to obtain sulfur and SO2-containing Claus tail gas, carrying out hydrogenation reduction on the Claus tail gas to convert SO2 into H2S, to obtain hydrogenated process gas, and after transferring heat of the hydrogenated process gas with quenched water, carrying out solvent desulfurization treatment; and (2) carrying out hydrofining treatment of raw oil, to obtain a refined product, mixing the refined product with washing water, injecting water into the mixture to obtain a water-injected refined product, and separating the hydrofined product from the water-injected refined product. The method is characterized in that the washing water contains the heat-transferred quenched water in the step (1). Through the above technical schemes, the method has relatively low operating costs.
Description
Technical field
The present invention relates to the derived energy chemical field, particularly, relate to a kind of method of coproduction sulphur and hydrofining product.
Background technology
Usually contain a certain amount of element sulphur in coal, oil and natural gas, these element sulphurs are collected as the sour gas that contains hydrogen sulfide in Coal Chemical Industry, petroleum refining and natural gas conditioning process.In order effectively to reclaim sulphur and to reduce environmental, usually by recovery technology of sulfur, the element sulphur in above-mentioned sour gas is converted into to sulphur, and by the SO in tail gas
2it is below the mark that concentration is reduced to safety dumping.
Crouse (CLAUS) method is the recovery technology of sulfur be most widely used at present, and the method is by British CF Crouse in invention in 1883, and its principle is to make the hydrogen sulfide incomplete combustion, then the sulfurous gas that makes to generate reacts with hydrogen sulfide and generates sulphur.
The sulfurous gas (2000-3000ppm) that also contains some amount in the tail gas that Kraus process is discharged, in order to meet the requirement of GB16297-1996 " discharge standard of air pollutants ", also need Claus tail gases is processed, make finally to enter in the tail gas of atmosphere containing amount of sulfur dioxide below 334ppm, the total yield of sulphur is reached more than 99.8%.The claus tail-gas clean-up method be most widely used mainly comprises: described Claus tail gases is carried out to hydrogenating reduction, cooling and solvent desulfurization processing.
In existing recovery technology of sulfur, Claus tail gases after hydrogenating reduction is carried out coolingly by with quenched water, carrying out heat exchange, realizing, contain the hydrogen sulfide that concentration is 150-300mg/L in quenched water after heat exchange, therefore need to carry out could discharging after the desulfurization of sewage air lift, there is the higher defect of quenched water processing cost after heat exchange in existing recovery technology of sulfur.
Hydrofining refers under hydrogen pressure and catalyzer exist, and makes the detrimental impurity such as sulphur, oxygen and nitrogen in oil product change corresponding hydrogen sulfide, water and ammonia into and remove, and make alkene and diene hydrogenation saturated and make the process that the aromatic hydrocarbons partial hydrogenation is saturated.Hydrofining can make the impurity of stock oil reduce and quality improves, obtain the hydrofining product, its method mainly comprises: stock oil is carried out to the hydrofining processing, obtain refined products, and described refined products is mixed to laggard horizontal high voltage air cooling and hydrofining product separation with washing water.
In existing hydrofining technology, the fresh de-mineralized water that the source of washing water is the system supply, and be difficult to recycle, therefore existing hydrofining technology exists washing water to use and the higher defect of processing cost.
Summary of the invention
The objective of the invention is to overcome existing recovery technology of sulfur and have the defect that quenched water processing cost after heat exchange is higher and overcome existing hydrofining technology simultaneously and exist washing water to use and the higher defect of processing cost, coproduction sulphur that a kind of running cost is lower and the method for hydrofining product are provided.
To achieve these goals, the invention provides a kind of method of coproduction sulphur and hydrofining product, the following steps that the method comprises successively or carries out simultaneously:, under the claus reaction condition, the sour gas that will contain hydrogen sulfide contacts with oxygen-containing gas (1), obtains sulphur and contains SO
2claus tail gases, described Claus tail gases is carried out to hydrogenating reduction with by SO
2be converted into H
2s, obtain the Process Gas after hydrogenation, and will carry out solvent desulfurization processing after the Process Gas after described hydrogenation and quenched water heat exchange; (2) stock oil is carried out to the hydrofining processing, obtain refined products, and described refined products is mixed with washing water carry out water filling, obtain the refined products after water filling, and separate the hydrofining product from the refined products described water filling; It is characterized in that, described washing water contain the quenched water after (1) middle heat exchange in steps.
By technique scheme, can save the step of the quenched water after heat exchange being carried out to the air lift desulfurization, and reduce the consumption of fresh washing water, therefore there is lower running cost.
Other features and advantages of the present invention will partly be described in detail in embodiment subsequently.
The accompanying drawing explanation
Accompanying drawing is to be used to provide a further understanding of the present invention, and forms the part of specification sheets, is used from explanation the present invention with following embodiment one, but is not construed as limiting the invention.In the accompanying drawings:
Fig. 1 is the schema of the method for coproduction sulphur provided by the invention and hydrofining product.
Fig. 2 is a kind of schema of preferred implementation of the method for coproduction sulphur provided by the invention and hydrofining product.
Description of reference numerals
100 pipeline 101 pipeline 102 pipelines
103 pipeline 104 pipeline 105 pipelines
106 pipeline 107 pipeline 108 pipelines
109 pipeline 110 pipelines
200 first hydrofining reactor 201 second hydrofining reactors
202 process furnace 203 heat exchangers
300 pipeline 301 pipeline 302 pipelines
303 pipeline 304 pipelines
400 roasting kiln 401 claus reaction devices
402 claus reaction device 403 water coolers
404 water coolers
500 pipeline 501 pipeline 502 pipelines
503 pipeline 504 pipeline 505 pipelines
506 pipeline 507 pipeline 508 pipelines
509 pipelines
600 desulphurization of recycle hydrogen device 601 knockout towers
602 high-pressure air cooler 603 air lift thionizers
604 separation columns
700 pipeline 701 pipeline 702 pipelines
703 pipeline 704 pipeline 705 pipelines
706 pipeline 707 pipelines
800 quench tower 801 hydrogenating reduction towers
802 well heater 803 solvent thionizers
804 solvent recovery towers
900 pipelines
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is elaborated.Should be understood that, embodiment described herein only, for description and interpretation the present invention, is not limited to the present invention.
The invention provides a kind of method of coproduction sulphur and hydrofining product, the following steps that the method comprises successively or carries out simultaneously:, under the claus reaction condition, the sour gas that will contain hydrogen sulfide contacts with oxygen-containing gas (1), obtains sulphur and contains SO
2claus tail gases, described Claus tail gases is carried out to hydrogenating reduction with by SO
2be converted into H
2s, obtain the Process Gas after hydrogenation, and will carry out solvent desulfurization processing after the Process Gas after described hydrogenation and quenched water heat exchange; (2) stock oil is carried out to the hydrofining processing, obtain refined products, and described refined products is mixed with washing water carry out water filling, obtain the refined products after water filling, and separate the hydrofining product from the refined products described water filling; It is characterized in that, described washing water contain the quenched water after (1) middle heat exchange in steps.
Typically, the method for coproduction sulphur provided by the invention and hydrofining product can be by the flowcharting shown in Fig. 1.
Wherein, described claus reaction is to instigate the hydrogen sulfide incomplete combustion, then makes the sulfurous gas that generates and hydrogen sulfide that anti-disproportionation reaction occur and generate the chemical reaction of sulphur and water.The routine that described claus reaction condition is this area is selected, and the present invention does not have special requirement, as long as meet, can make to contain SO in described Claus tail gases
2get final product, such as being the claus reaction condition of record in document (Chen Gengliang etc., " Claus sulfur recovery Technology ", petroleum industry press, 2007).Contain SO
2claus tail gases can use SCOT tail gas treatment process (for example, described in document (Diao Jiuhua, SCOT tail gas of sulphur treatment technology improves summary, gas sweetening and sulphur recovery, the 2nd phase in 2006)) to carry out purifying treatment.It should be noted that, in the Claus tail gases that super claus reaction (for example, described in document (Wang Jiaming, super Crouse's recovery technology of sulfur and application, Sweet natural gas and oil, the 27th volume, the 5th phase in 2009)) obtains, contain H
2s and do not contain SO
2, thereby be not suitable for the SCOT tail gas treatment process, be not suitable for carrying out hydrogenating reduction.
Wherein, typically, described claus reaction condition comprises: make hydrogen sulfide in the unburnt stage, temperature is 1000-1400 ℃, is preferably 1100-1350 ℃, and pressure is 0.010-0.040MPa, is preferably 0.020-0.030MPa.Reaction time is in 1-2 second.Can be considered moment completes.Make during the stage of anti-disproportionation reaction occurs sulfurous gas and hydrogen sulfide, temperature is 200-250 ℃, is preferably 220-250 ℃, and pressure is 0.001-0.020MPa, is preferably 0.002-0.003MPa.Reaction time is in 1-2 second.Can be considered moment completes.Described claus reaction condition can also comprise: anti-disproportionation reaction can be carried out under catalyzer exists, this catalyzer can be the various catalyzer that are applicable to claus reaction that are purchased, for example can for purchased from become can be special the trade names catalyzer that be CT6-2B, purchased from least one in the catalyzer that becomes the trade names catalyzer that is CT6-4B that can be special and be LS-300 purchased from the trade names of Shandong section power.
Wherein, the material that anti-disproportionation reaction can be obtained is cooled to 130-150 ℃, then carries out gas-liquid separation, obtains Molten sulphur and remaining gas.
Wherein, described remaining gas can also be contacted with catalyzer again under the claus reaction condition, to carry out the next stage claus reaction, thereby the hydrogen sulfide in the raising sour gas is converted into the transformation efficiency of sulphur.That is, can carry out multistage claus reaction, usually can carry out 2-4 level claus reaction, preferably carry out 4 grades of claus reactions.The condition of multistage claus reaction can be identical, also can be different, as long as claus reaction can occur.
Wherein, the condition of described Claus tail gases being carried out to hydrogenating reduction can be the selection of this area routine, as long as can be by the SO in Claus tail gases
2hydrogenating reduction becomes H
2s gets final product, and the present invention does not have special requirement, for example, and the condition described in document (Diao Jiuhua, SCOT tail gas of sulphur treatment technology improves summary, gas sweetening and sulphur recovery, the 2nd phase in 2006).
Wherein, typically, the condition of described Claus tail gases being carried out to hydrogenating reduction can comprise: temperature is 240-320 ℃, is preferably 240-260 ℃, and pressure is 0.001-0.015MPa, is preferably 0.004-0.005MPa.Reaction time is in 1-2 second.Can be considered moment completes.The catalyzer of hydrogenating reduction can be the various catalyzer that are applicable to the hydrogenation reduction of Claus tail gases that are purchased, and can be for example at least one in the catalyzer purchased from becoming the trade names catalyzer that be CT-5B that can be special, the catalyzer that is LS-951Q purchased from the trade names of Shandong section power and being TG107 purchased from the trade names of Axens company.
Wherein, typically, by in the process of the Process Gas after described hydrogenation and quenched water heat exchange, the starting temperature of the Process Gas after hydrogenation can be 245-280 ℃, the starting temperature of quenched water can be 30-40 ℃, the temperature of Process Gas after hydrogenation after heat exchange can be 35-45 ℃, and the temperature of the quenched water after heat exchange can be 40-55 ℃.Wherein, the Process Gas after described hydrogenation can be for directly contacting with the mode of quenched water heat exchange.Wherein, Process Gas after described hydrogenation is in situation about directly contacting with the mode of quenched water heat exchange, method of the present invention also is included in solvent desulfurization after heat exchange removes the Process Gas after heat exchange water before processing, the Process Gas removed after water is carried out to solvent desulfurization processing, by isolated water as described water filling.
Wherein, described quenched water can, for the various process waters that are suitable for the Process Gas after cooling described hydrogenation, be preferably hardness at the process water below 1.Wherein, hardness refers to that method by standard GB/T 7477-87 regulation records the numerical value (the Ca element of every 1ppmw is 1 hardness value) that the weight content of Ca element means of take obtained.Wherein, process water refers to the water of the water quality standard that meets standard GB/T/T19923-2005 regulation.Wherein, can by the method for conventional reduction water hardness, make industrial water hardness be down to below 1.
Wherein, will after the Process Gas after described hydrogenation and quenched water heat exchange, carry out in the process of solvent desulfurization processing, the condition of solvent desulfurization does not have special requirement, can be selection conventional in the SCOT method.Typically, the solvent desulfurization is processed and carried out under the following conditions: temperature is 25-45 ℃.For the solvent of solvent desulfurization, can be conventional selection, for example, purchased from the MEDA(methyldiethanolamine of Nanjing chemical industry) solvent, the MEDA(methyldiethanolamine purchased from Qingdao with hat) solvent and purchased from the MEDA(methyldiethanolamine of Jiangyin Golden Horse) at least one in solvent.The solvent desulfurization can be collected the hydrogen sulfide in the Process Gas after described hydrogenation in solvent, the solvent of having collected hydrogen sulfide can obtain fresh solvent and H 2 S-containing gas by conventional method for regenerating solvent regeneration, this hydrogen sulfide can be incorporated in sour gas as above, proceeds the operation of recovery sulphur.Process Gas after described hydrogenation is by after the solvent desulfurization, residual a certain amount of waste gas also, and this waste gas can be burned by conventional incinerating method rear discharge.
Wherein, the method for stock oil being carried out to the hydrofining processing can be the selection of this area routine, and the present invention does not have special requirement, as long as wherein relate to the step that described refined products is mixed to carry out water filling with washing water.
Wherein, described washing water refer to conventional for described refined products being carried out to the water of water filling with the water-soluble impurity of removing refined products; Described water-soluble impurity generally includes ammonia nitrogen, chlorion and hydrogen sulfide etc.
The method according to this invention, wherein, described temperature of washing water meets requirement convenient and that be suitable for mixing with described refined products carrying out water filling and gets final product.Typically, the temperature of described washing water can be 20-50 ℃, is preferably 30-40 ℃.
The present inventor finds, the water quality of the quenched water in step (1) after heat exchange meets the water quality standard of hydrofining technology to washing water fully, thereby the quenched water after heat exchange in step (1) can be used as to the washing water of step (2), the subsequent disposal problem of quenched water in like this can settlement steps to deal (1), thereby solve the source problem that comes of washing water, reach the effect of water saving.Hydrofining technology is well known to a person skilled in the art to the water quality standard of washing water, for example, disclosed washing water quality standard in international standard API 932-B (content of ammonia nitrogen is below 1000ppmw, and the content of element sulphur is below 1000ppmw, and the content of chlorine element is that 5ppmw is following).Typically, in the quenched water in step (1) after heat exchange, the content of ammonia nitrogen is 200-800mg/L, is preferably 200-500mg/L; The content of element sulphur is 150-300mg/L, is preferably 150-200mg/L, and the content of chlorine element is 0.001-4mg/L, is preferably 0.01-1mg/L.
The method according to this invention, wherein, described washing water can be the quenched water after heat exchange in step (1).That is, described washing water can be all in step (1) quenched water after heat exchange substituted.In addition, described washing water can be also the mixture of the quenched water after heat exchange in process water and step (1).
The method according to this invention, wherein, with respect to the described refined products of 1 weight part, the consumption of described washing water can be the 0.05-0.3 weight part, is preferably the 0.1-0.2 weight part.
The method according to this invention, wherein, the method for extracting the hydrofining product from described mixed material does not have special requirement, can be the selection in conventional hydrofining technology.Typically, from described mixed material, the method for extraction hydrofining product comprises: the refined products after described water filling is carried out to high pressure air cooling, oily water separation, air lift desulfurization and fractionation successively.
Wherein, described high pressure air cooling can carry out under conventional high pressure air cooling condition, for example, can be (preferably under 3.4-3.75MPa) under 3.3-3.8MPa at pressure, and the temperature of the refined products after described water filling is cooled to 30-40 ℃ from 160-180 ℃.Material after the high pressure air cooling can have oil, the gentle three-phase of water.Gaseous phase materials can separate through gas-liquid separation.Oil phase material and water material can be with separating by oily water separation.The gentle phase materials of water material can further carry out conventional purification and/or recycling.
Wherein, described oily water separation can be carried out under conventional oily water separation condition.The oil phase obtained after oily water separation can carry out air lift desulfurization processing, to remove the sulfocompound (as hydrogen sulfide) wherein dissolved.Carry out refined products after air lift desulfurization processing and can be used as hydrofining product (as-10# diesel oil), also can further carry out the hydrofining product that conventional fractionation obtains including but not limited to dry gas, oil liquefied gas, light naphthar, heavy naphtha, aviation kerosene, diesel oil and tail oil.
The method according to this invention, wherein, described stock oil can be for various routines can be used for hydrorefined raw material, typically, described stock oil can contain coking oil and straight-run diesel oil, and the weight ratio of coking oil and straight-run diesel oil is 1:5-20, described stock oil can be also at least one in straight-run spirit, coker gasoline and non-aromatics.Above-mentioned coking oil, straight-run diesel oil, straight-run spirit, coker gasoline and non-aromatics all have definition well known in the art.
The method according to this invention, wherein, typically, in described Claus tail gases, SO
2content can be 0.2-0.3 volume %.
The method according to this invention, wherein, in described sour gas, the content of hydrogen sulfide does not have special requirement, can be the selection of this area routine, and typically, in described sour gas, the content of hydrogen sulfide can be 75-95 volume %.
The method according to this invention, wherein, the hydrogen sulfide in described sour gas partly or entirely derives from the operation of extracting the hydrofining product in step (2) from the refined products described water filling.Particularly, can the sulfocompound in gaseous phase materials as above and oil phase material (as hydrogen sulfide) be collected into by conventional method as described in sour gas.
Below, with reference to Fig. 2, illustrate the particularly preferred a kind of embodiment of the present invention.
Sour gas (hydrogen sulfide content is 75-95 volume %) enters burner 400 through pipeline 100, pipeline 101 and pipeline 102, and pass into air (mol ratio of the hydrogen sulfide in airborne oxygen and sour gas is 1:0.55-0.60) through pipeline 300, in burner 400, the incomplete combustion of hydrogen sulfide occurs, temperature is 1100-1200 ℃, pressure is 0.020-0.030MPa, and the time is 1-2 second, material in burner 400 (is the material after the hydrogen sulfide incomplete combustion in sour gas, contains SO
2and hydrogen sulfide) enter claus reaction device 401(as first step claus reaction device), in claus reaction device 401, anti-disproportionation reaction occurs in sulfurous gas and hydrogen sulfide, temperature is 220-250 ℃, pressure is 0.002-0.003MPa, the catalyzer of anti-disproportionation reaction for purchased from become can be special the trade names catalyzer that is CT6-2B, purchased from least one in the catalyzer that becomes the trade names catalyzer that is CT6-4B that can be special and be LS-300 purchased from the trade names of Shandong section power, material after anti-disproportionation reaction (occurs in the material in claus reaction device 401, contain sulphur and remaining unreacted gas completely) enter water cooler 403 and be cooled to 130-150 ℃, sulphur and remaining unreacted gas are completely separated, sulphur exports to the molten sulfur pond through pipeline 301, unreacted completely gas after pipeline 302 is derived, successively enter claus reaction device 402 and water cooler 404, with the claus reaction that carries out next stage, with sulphur, separate, this step repeats 3 times, carry out altogether 4 grades of claus reactions, in claus reactions at different levels, the molten sulfur pond can share, be that sulphur in pipeline 301 and pipeline 303 can import in same molten sulfur pond, after 4 grades of claus reactions finish, remaining gas is the Claus tail gases (SO that wherein contains 0.2-0.3 volume %
2), Claus tail gases can be derived through pipeline 304.
Claus tail gases in pipeline 304 is imported in well heater 802, after being heated to 240-260 ℃, import hydrogenation reduction device 801 through pipeline 703, in hydrogenation reduction device 801, temperature is 240-260 ℃, pressure is 0.004-0.005MPa, and the catalyzer of hydrogenating reduction is at least one in the catalyzer purchased from becoming the trade names catalyzer that is CT-5B that can be special, the catalyzer that is LS-951Q purchased from the trade names of Shandong section power and being TG107 purchased from the trade names of A xens company, Process Gas after described hydrogenation is directed in quench tower 800 through pipeline 702, and directly contact and carry out the caloic exchange and obtain chilling by the quenched water (hardness is at the process water below 1) with import quench towers 800 through pipeline 700, the starting temperature of the Process Gas after hydrogenation is 245-280 ℃, the starting temperature of quenched water is 30-40 ℃, making the temperature of Process Gas after heat exchange after hydrogenation by the consumption of controlling quenched water is 35-45 ℃, the temperature of the quenched water after heat exchange improves 5-25 ℃ (being for example 40-55 ℃) than starting temperature, through pipeline 900, derives, Process Gas after hydrogenation is directed into solvent thionizer 803 in heat exchange by pipeline 701, in solvent thionizer 803, solvent (as MEDA) is by the hydrogen sulfide stripping in the Process Gas after hydrogenation, obtain being dissolved with solvent and the waste gas of hydrogen sulfide, the solvent that is dissolved with hydrogen sulfide imports in solvent recovery tower 804 through pipeline 705, in solvent recovery tower 804, to be dissolved with hydrogen sulfide and separated from solvent in the solvent of hydrogen sulfide by gas stripping process, the solvent be recycled and the waste gas that contains hydrogen sulfide, recovered solvent can be used as fresh solvent or mixes by pipeline 707 and be back to solvent thionizer 803 with fresh solvent, the waste gas that contains hydrogen sulfide is discharged through pipeline 704, discharge after burning.
The hydrogen that will import through pipeline 109 and 110 (as the 5.5-6.5 ten thousand stere/hour) and the stock oil (straight-run spirit that imports through pipeline 103, as the 70-90 ton/hour) mix, mixed material, through pipeline 108 delivery heat exchangers 203, carries out heat exchange with the refined products imported through pipeline 105 in heat exchanger 203, above-mentioned mixed material through heat exchange imports in process furnace 202 and is heated to 230-250 ℃ through pipeline 107, and import the first hydrofining reactor 200 by pipeline 104, in the first hydrofining reactor 200, temperature is 220-290 ℃, pressure is 3.7-3.9MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), product in the first hydrofining reactor imports the second hydrofining reactor 201 through pipeline 106, in the second hydrofining reactor 201, temperature is 260-340 ℃, pressure is 3.65-3.85MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), product in the second hydrofining reactor carries out heat exchange with hydrogen and the mixed material of stock oil in pipeline 105 delivery heat exchangers 203, then through pipeline 508, derive, and mix (with respect to the described refined products of 1 weight part with washing water (be the heat exchange in pipeline 900 after quenched water), the consumption of described washing water is the 0.1-0.2 weight part), then import in high-pressure air cooler 602 and carry out the high pressure air cooling through pipeline 507, the condition of high pressure air cooling is at pressure being (preferably under 3.4-3.75MPa) under 3.3-3.8MPa, the temperature of the refined products after described water filling is cooled to 30-40 ℃ from 160-180 ℃, material after the high pressure air cooling enters in knockout tower 601 through pipeline 602, separate and obtain gaseous phase materials, oil phase material and water material, gaseous phase materials imports desulphurization of recycle hydrogen device 600 through pipeline 502, in desulphurization of recycle hydrogen device 600, make hydrogen sulfide and the Hydrogen Separation in gaseous phase materials by the solvent doctor treatment, hydrogen sulfide imports in the sour gas of pipelines 102 and operates for recovery sulphur through pipeline 501, hydrogen imports in the hydrogen in pipelines 109 and operates for hydrofining through pipeline 509, the water material is discharged through pipeline 504, oil phase material imports air lift devulcanizer 603 through pipeline 503, in air lift devulcanizer 603, the hydrogen sulfide dissolved in oil phase material is separated and enter pipeline 500, in the sour gas of the hydrogen sulfide remittance pipeline 102 in pipeline 500 and for the recovery sulphur operation, remaining oil phase material can obtain the hydrofining product after in pipeline 505 importing fractionators 604, carrying out fractionation.
Further describe by the following examples the present invention.In following examples and reference example, stock oil is identical, is coker gasoline and the non-aromatics mixture that 7:3 obtains after mixing by weight, and wherein, the character of coker gasoline and non-aromatics is as shown in table 1.Wherein, each index is all undertaken by the standard of announcing, and for example: the mensuration of density is undertaken by GB/T 13377-1992; The mensuration of boiling range is undertaken by GB-T 255-77; The mensuration of bromine valency is undertaken by GB/T 11136-1989; The mensuration of nitrogen content is carried out according to SH/T0171-1992 (2007); The mensuration of sulphur content is carried out according to SH/T 0172-2001; Aromaticity content carries out according to SH/T 0177-1992 (2007).
Table 1
With reference to Fig. 2, sour gas (hydrogen sulfide content is 85 volume %) enters burner 400 through pipeline 100, pipeline 101 and pipeline 102, and pass into air (mol ratio of the hydrogen sulfide in airborne oxygen and sour gas is 1:0.57) through pipeline 300, in burner 400, the incomplete combustion of hydrogen sulfide occurs, temperature in burner 400 is 1150 ℃, and pressure is 0.025MPa, and the residence time of sour gas in burner was 1.5 seconds, material in burner 400 (is the material after the hydrogen sulfide incomplete combustion in sour gas, contains SO
2and hydrogen sulfide) enter claus reaction device 401(as first step claus reaction device), in claus reaction device 401, anti-disproportionation reaction occurs in sulfurous gas and hydrogen sulfide, and the temperature in claus reaction device 401 is 240 ℃, pressure is 0.0025MPa, and the volume space velocity of gas is 1500 hours
-1, the catalyzer of anti-disproportionation reaction for purchased from become can be special the trade names catalyzer that is CT6-2B, material after anti-disproportionation reaction (occurs in the material in claus reaction device 401, contain sulphur and remaining unreacted gas completely) entering water cooler 403, to be cooled to temperature be 140 ℃, sulphur and remaining unreacted gas are completely separated, sulphur exports to the molten sulfur pond through pipeline 301, unreacted completely gas after pipeline 302 is derived, successively enter claus reaction device 402 and water cooler 404, with the claus reaction that carries out next stage, with sulphur, separate, this step repeats 3 times, carry out altogether 4 grades of claus reactions, in claus reactions at different levels, reaction conditions (temperature, pressure, volume space velocity and catalyzer) identical, the molten sulfur pond shares, be that sulphur in pipeline 301 and pipeline 303 imports in same molten sulfur pond, after 4 grades of claus reactions finish, remaining gas is the Claus tail gases (SO that wherein contains 0.25 volume %
2), Claus tail gases is derived through pipeline 304.
Claus tail gases in pipeline 304 is imported in well heater 802, after being heated to temperature and being 250 ℃, import hydrogenation reduction device 801 through pipeline 703, temperature in hydrogenation reduction device 801 is 250 ℃, pressure is 0.0045MPa, the catalyzer of hydrogenating reduction for purchased from become can be special the trade names catalyzer that is CT-5B, the volume space velocity of gas is 1500 hours
-1, Process Gas after described hydrogenation is directed into quench tower 800 from the bottom of quench tower 800 through pipeline 702, and by the quenched water (process water that hardness is 0.8) with import quench tower 800 from the top of quench tower 800 through pipeline 700 directly counter current contact carry out the caloic exchange and obtain chilling, the starting temperature of the Process Gas after hydrogenation is 265 ℃, the starting temperature of quenched water is 35 ℃, making the temperature of Process Gas after heat exchange after hydrogenation by the consumption of controlling quenched water is 40 ℃, the temperature of the quenched water after heat exchange improves 15 ℃ (being 50 ℃) than starting temperature, through pipeline 900, derive, Process Gas after hydrogenation is directed into solvent thionizer 803 in heat exchange by pipeline 701, in solvent thionizer 803, solvent (purchased from the MEDA(methyldiethanolamine of Nanjing chemical industry) solvent) by the hydrogen sulfide stripping in the Process Gas after hydrogenation, obtain being dissolved with solvent and the waste gas of hydrogen sulfide, the solvent that is dissolved with hydrogen sulfide imports in solvent recovery tower 804 through pipeline 705, in solvent recovery tower 804, to be dissolved with hydrogen sulfide and separated from solvent in the solvent of hydrogen sulfide by gas stripping process, the solvent be recycled and the waste gas that contains hydrogen sulfide, recovered solvent mixes by pipeline 707 and is back to solvent thionizer 803 with fresh solvent, the waste gas that contains hydrogen sulfide is discharged through pipeline 704, discharge after burning.
Wherein, after measured, in the quenched water after heat exchange (being the quenched water after the heat exchange in pipeline 900), the content of ammonia nitrogen is 350mg/L; The content of element sulphur is 180mg/L, and the content of chlorine element is 0.5mg/L, meets disclosed washing water quality standard-required in international standard API 932-B.Wherein, the content of ammonia nitrogen is measured according to GB/T 12146-2005, and the content of element sulphur is measured according to GB/T 6911-2007, and the content of chlorine element is measured according to GB/T 15453-2008.
The hydrogen that will import through pipeline 109 and 110 (6 ten thousand steres/hour) and the stock oil (80 tons/hour) imported through pipeline 103 mix, mixed material, through pipeline 108 delivery heat exchangers 203, carries out heat exchange with the refined products imported through pipeline 105 in heat exchanger 203, it is 240 ℃ that the above-mentioned mixed material of process heat exchange is heated to temperature in pipeline 107 importing process furnace 202, and import the first hydrofining reactor 200 by pipeline 104, in the first hydrofining reactor 200, temperature is 250 ℃, pressure is 3.8MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), and the volume space velocity of stock oil is 2.0 hours
-1, product in the first hydrofining reactor imports the second hydrofining reactor 201 through pipeline 106, in the second hydrofining reactor 201, temperature is 300 ℃, pressure is 3.75MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), product in the second hydrofining reactor carries out heat exchange with hydrogen and the mixed material of stock oil in pipeline 105 delivery heat exchangers 203, then through pipeline 508, derive, and mix (with respect to the described refined products of 1 weight part with washing water (be the heat exchange in pipeline 900 after quenched water), the consumption of described washing water is 0.15 weight part), then import in high-pressure air cooler 602 and carry out the high pressure air cooling through pipeline 507, the condition of high pressure air cooling is is under 3.55MPa at pressure, the temperature of the refined products after described water filling is cooled to 35 ℃ from 170 ℃, material after the high pressure air cooling enters in knockout tower 601 through pipeline 602, separate and obtain gaseous phase materials, oil phase material and water material, gaseous phase materials imports desulphurization of recycle hydrogen device 600 through pipeline 502, in desulphurization of recycle hydrogen device 600, make hydrogen sulfide and the Hydrogen Separation in gaseous phase materials by the solvent doctor treatment, hydrogen sulfide imports in the sour gas of pipelines 102 and operates for recovery sulphur through pipeline 501, hydrogen imports in the hydrogen in pipelines 109 and operates for hydrofining through pipeline 509, the water material is discharged through pipeline 504, oil phase material imports air lift devulcanizer 603 through pipeline 503, in air lift devulcanizer 603, the hydrogen sulfide dissolved in oil phase material is separated and enter pipeline 500, hydrogen sulfide in pipeline 500 imports in the sour gas of pipeline 102 and operates for recovery sulphur, remaining oil phase material obtains the hydrofining product after in pipeline 505 importing fractionators 604, carrying out fractionation, and the character of this hydrofining product is as shown in table 1.
After moving three months according to the method described above, not finding has substantial obstruction and corrosion phenomenon in the pipeline of hydrofining technology, and the technique overall operation is good.Illustrate thus the present invention adopt with described hydrogenation after the Process Gas heat exchange after quenched water as the water filling of hydrotreated product, be feasible, can greatly reduce the demand of hydrofining technology to fresh water thus, and reduce the water treatment expense.
Reference example 1
Method according to embodiment 1 is carried out the hydrofining processing to crude oil, different, the fresh de-mineralized water that washing water are the system supply.The character of this hydrofining product is as shown in table 1.
Compare and can find out by the hydrofining product by embodiment 1 and reference example 1 acquisition, the quality of the two is suitable, and the quenched water after the Process Gas heat exchange after explanation and described hydrogenation can be used as the washing water use that hydrofining is processed fully thus.
Embodiment 2
With reference to figure 2, sour gas (hydrogen sulfide content is 90 volume %) enters burner 400 through pipeline 100, pipeline 101 and pipeline 102, and pass into air (mol ratio of the hydrogen sulfide in airborne oxygen and sour gas is 1:0.59) through pipeline 300, in burner 400, the incomplete combustion of hydrogen sulfide occurs, temperature in burner 400 is 1180 ℃, and pressure is 0.028MPa, and the residence time of sour gas in burner was 1.8 seconds, material in burner 400 (is the material after the hydrogen sulfide incomplete combustion in sour gas, contains SO
2and hydrogen sulfide) enter claus reaction device 401(as first step claus reaction device), in claus reaction device 401, anti-disproportionation reaction occurs in sulfurous gas and hydrogen sulfide, and the temperature in claus reaction device 401 is 245 ℃, pressure is 0.0028MPa, and the volume space velocity of gas is 1500 hours
-1, the catalyzer that the catalyzer of anti-disproportionation reaction is LS-300 for the trade names purchased from Shandong section power, material after anti-disproportionation reaction (occurs in the material in claus reaction device 401, contain sulphur and remaining unreacted gas completely) entering water cooler 403, to be cooled to temperature be 145 ℃, sulphur and remaining unreacted gas are completely separated, sulphur exports to the molten sulfur pond through pipeline 301, unreacted completely gas after pipeline 302 is derived, successively enter claus reaction device 402 and water cooler 404, with the claus reaction that carries out next stage, with sulphur, separate, this step repeats 3 times, carry out altogether 4 grades of claus reactions, in claus reactions at different levels, reaction conditions (temperature, pressure, volume space velocity and catalyzer) identical, the molten sulfur pond shares, be that sulphur in pipeline 301 and pipeline 303 imports in same molten sulfur pond, after 4 grades of claus reactions finish, remaining gas is the Claus tail gases (SO that wherein contains 0.28 volume %
2), Claus tail gases is derived through pipeline 304.
Claus tail gases in pipeline 304 is imported in well heater 802, after being heated to temperature and being 258 ℃, import hydrogenation reduction device 801 through pipeline 703, temperature in hydrogenation reduction device 801 is 258 ℃, pressure is 0.0048MPa, the catalyzer that the catalyzer of hydrogenating reduction is TG107 for the trade names purchased from A xens company, the volume space velocity of gas is 1500 hours
-1, Process Gas after described hydrogenation is directed in quench tower 800 through pipeline 702, and by the quenched water (process water that hardness is 0.6) with import quench tower 800 from the top of quench tower 800 through pipeline 700 directly counter current contact carry out the caloic exchange and obtain chilling, the starting temperature of the Process Gas after hydrogenation is 270 ℃, the starting temperature of quenched water is 32 ℃, making the temperature of Process Gas after heat exchange after hydrogenation by the consumption of controlling quenched water is 45 ℃, the temperature of the quenched water after heat exchange improves 20 ℃ (being 52 ℃) than starting temperature, through pipeline 900, derives, Process Gas after hydrogenation is directed into solvent thionizer 803 in heat exchange by pipeline 701, in solvent thionizer 803, solvent (purchased from the MEDA(methyldiethanolamine of Jiangyin Golden Horse) solvent) by the hydrogen sulfide stripping in the Process Gas after hydrogenation, obtain being dissolved with solvent and the waste gas of hydrogen sulfide, the solvent that is dissolved with hydrogen sulfide imports in solvent recovery tower 804 through pipeline 705, in solvent recovery tower 804, to be dissolved with hydrogen sulfide and separated from solvent in the solvent of hydrogen sulfide by gas stripping process, the solvent be recycled and the waste gas that contains hydrogen sulfide, recovered solvent mixes by pipeline 707 and is back to solvent thionizer 803 with fresh solvent, the waste gas that contains hydrogen sulfide is discharged through pipeline 704, discharge after burning.
Wherein, after measured, in the quenched water after heat exchange (being the quenched water after the heat exchange in pipeline 900), the content of ammonia nitrogen is 450mg/L; The content of element sulphur is 190mg/L, and the content of chlorine element is 0.9mg/L, meets disclosed washing water quality standard-required in international standard API 932-B.Wherein, the content of ammonia nitrogen is measured according to GB/T 12146-2005, and the content of element sulphur is measured according to GB/T 6911-2007, and the content of chlorine element is measured according to GB/T 15453-2008.
The hydrogen that will import through pipeline 109 and 110 (6.3 ten thousand steres/hour) and the stock oil (75 tons/hour) imported through pipeline 103 mix, mixed material, through pipeline 108 delivery heat exchangers 203, carries out heat exchange with the refined products imported through pipeline 105 in heat exchanger 203, it is 245 ℃ that the above-mentioned mixed material of process heat exchange is heated to temperature in pipeline 107 importing process furnace 202, and import the first hydrofining reactor 200 by pipeline 104, in the first hydrofining reactor 200, temperature is 280 ℃, pressure is 3.8MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), product in the first hydrofining reactor imports the second hydrofining reactor 201 through pipeline 106, and the volume space velocity of stock oil is 2.0 hours
-1, in the second hydrofining reactor 201, temperature is 330 ℃, pressure is 3.8MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), product in the second hydrofining reactor carries out heat exchange with hydrogen and the mixed material of stock oil in pipeline 105 delivery heat exchangers 203, then through pipeline 508, derive, and mix (with respect to the described refined products of 1 weight part with washing water (be the heat exchange in pipeline 900 after quenched water), the consumption of described washing water is 0.18 weight part), then import in high-pressure air cooler 602 and carry out the high pressure air cooling through pipeline 507, the condition of high pressure air cooling is is under 3.7MPa at pressure, the temperature of the refined products after described water filling is cooled to 38 ℃ from 175 ℃, material after the high pressure air cooling enters in knockout tower 601 through pipeline 602, separate and obtain gaseous phase materials, oil phase material and water material, gaseous phase materials imports desulphurization of recycle hydrogen device 600 through pipeline 502, in desulphurization of recycle hydrogen device 600, make hydrogen sulfide and the Hydrogen Separation in gaseous phase materials by the solvent doctor treatment, hydrogen sulfide imports in the sour gas of pipelines 102 and operates for recovery sulphur through pipeline 501, hydrogen imports in the hydrogen in pipelines 109 and operates for hydrofining through pipeline 509, the water material is discharged through pipeline 504, oil phase material imports air lift devulcanizer 603 through pipeline 503, in air lift devulcanizer 603, the hydrogen sulfide dissolved in oil phase material is separated and enter pipeline 500, hydrogen sulfide in pipeline 500 imports in the sour gas of pipeline 102 and operates for recovery sulphur, remaining oil phase material obtains the hydrofining product after in pipeline 505 importing fractionators 604, carrying out fractionation, and the character of this hydrofining product is as shown in table 1.
After moving three months according to the method described above, not finding has substantial obstruction and corrosion phenomenon in the pipeline of hydrofining technology, and the technique overall operation is good.Illustrate thus the present invention adopt with described hydrogenation after the Process Gas heat exchange after quenched water as the water filling of hydrotreated product, be feasible, can greatly reduce the demand of hydrofining technology to fresh water thus, and reduce the water treatment expense.
Embodiment 3
With reference to Fig. 2, sour gas (hydrogen sulfide content is 78 volume %) enters burner 400 through pipeline 100, pipeline 101 and pipeline 102, and pass into air (mol ratio of the hydrogen sulfide in airborne oxygen and sour gas is 1:0.56) through pipeline 300, in burner 400, the incomplete combustion of hydrogen sulfide occurs, temperature in burner 400 is 1120 ℃, and pressure is 0.022MPa, and the residence time of sour gas in burner was 1.2 seconds, material in burner 400 (is the material after the hydrogen sulfide incomplete combustion in sour gas, contains SO
2and hydrogen sulfide) enter claus reaction device 401(as first step claus reaction device), in claus reaction device 401, anti-disproportionation reaction occurs in sulfurous gas and hydrogen sulfide, and the temperature in claus reaction device 401 is 230 ℃, pressure is 0.0022MPa, and the volume space velocity of gas is 1500 hours
-1, the catalyzer of anti-disproportionation reaction for purchased from become can be special the trade names catalyzer that is CT6-4B, material after anti-disproportionation reaction (occurs in the material in claus reaction device 401, contain sulphur and remaining unreacted gas completely) entering water cooler 403, to be cooled to temperature be 132 ℃, sulphur and remaining unreacted gas are completely separated, sulphur exports to the molten sulfur pond through pipeline 301, unreacted completely gas after pipeline 302 is derived, successively enter claus reaction device 402 and water cooler 404, with the claus reaction that carries out next stage, with sulphur, separate, this step repeats 3 times, carry out altogether 4 grades of claus reactions, in claus reactions at different levels, reaction conditions (temperature, pressure, volume space velocity and catalyzer) identical, the molten sulfur pond shares, be that sulphur in pipeline 301 and pipeline 303 imports in same molten sulfur pond, after 4 grades of claus reactions finish, remaining gas is the Claus tail gases (SO that wherein contains 0.22 volume %
2), Claus tail gases is derived through pipeline 304.
Claus tail gases in pipeline 304 is imported in well heater 802, after being heated to temperature and being 242 ℃, import hydrogenation reduction device 801 through pipeline 703, temperature in hydrogenation reduction device 801 is 242 ℃, pressure is 0.0042MPa, the catalyzer that the catalyzer of hydrogenating reduction is LS-951Q for the trade names purchased from Shandong section power, the volume space velocity of gas is 1500 hours
-1, Process Gas after described hydrogenation is directed in quench tower 800 through pipeline 702, and by the quenched water (process water that hardness is 0.7) with import quench tower 800 from the bottom of quench tower 800 through pipeline 700 directly counter current contact carry out the caloic exchange and obtain chilling, the starting temperature of the Process Gas after hydrogenation is 250 ℃, the starting temperature of quenched water is 30 ℃, making the temperature of Process Gas after heat exchange after hydrogenation by the consumption of controlling quenched water is 35 ℃, the temperature of the quenched water after heat exchange improves 5 ℃ (being 35 ℃) than starting temperature, through pipeline 900, derives, Process Gas after hydrogenation is directed into solvent thionizer 803 in heat exchange by pipeline 701, in solvent thionizer 803, solvent (purchased from the MEDA(methyldiethanolamine of Nanjing chemical industry) solvent) by the hydrogen sulfide stripping in the Process Gas after hydrogenation, obtain being dissolved with solvent and the waste gas of hydrogen sulfide, the solvent that is dissolved with hydrogen sulfide imports in solvent recovery tower 804 through pipeline 705, in solvent recovery tower 804, to be dissolved with hydrogen sulfide and separated from solvent in the solvent of hydrogen sulfide by gas stripping process, the solvent be recycled and the waste gas that contains hydrogen sulfide, recovered solvent mixes by pipeline 707 and is back to solvent thionizer 803 with fresh solvent, the waste gas that contains hydrogen sulfide is discharged through pipeline 704, discharge after burning.
Wherein, after measured, in the quenched water after heat exchange (being the quenched water after the heat exchange in pipeline 900), the content of ammonia nitrogen is 250mg/L; The content of element sulphur is 160mg/L, and the content of chlorine element is 0.2mg/L, meets disclosed washing water quality standard-required in international standard API 932-B.Wherein, the content of ammonia nitrogen is measured according to GB/T 12146-2005, and the content of element sulphur is measured according to GB/T 6911-2007, and the content of chlorine element is measured according to GB/T 15453-2008.
The hydrogen that will import through pipeline 109 and 110 (5.8 ten thousand steres/hour) and the stock oil (75 tons/hour) imported through pipeline 103 mix, mixed material, through pipeline 108 delivery heat exchangers 203, carries out heat exchange with the refined products imported through pipeline 105 in heat exchanger 203, it is 232 ℃ that the above-mentioned mixed material of process heat exchange is heated to temperature in pipeline 107 importing process furnace 202, and import the first hydrofining reactor 200 by pipeline 104, in the first hydrofining reactor 200, temperature is 230 ℃, pressure is 3.75MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), and the volume space velocity of stock oil is 2.0 hours
-1, product in the first hydrofining reactor imports the second hydrofining reactor 201 through pipeline 106, in the second hydrofining reactor 201, temperature is 280 ℃, pressure is 3.68MPa, catalyzer is FH-40 catalyzer (purchased from Sinopec Fushun Petrochemical Research Institute), product in the second hydrofining reactor carries out heat exchange with hydrogen and the mixed material of stock oil in pipeline 105 delivery heat exchangers 203, then through pipeline 508, derive, and mix (with respect to the described refined products of 1 weight part with washing water (be the heat exchange in pipeline 900 after quenched water), the consumption of described washing water is the 0.1-0.2 weight part), then import in high-pressure air cooler 602 and carry out the high pressure air cooling through pipeline 507, the condition of high pressure air cooling is is under 3.42MPa at pressure, the temperature of the refined products after described water filling is cooled to 32 ℃ from 165 ℃, material after the high pressure air cooling enters in knockout tower 601 through pipeline 602, separate and obtain gaseous phase materials, oil phase material and water material, gaseous phase materials imports desulphurization of recycle hydrogen device 600 through pipeline 502, in desulphurization of recycle hydrogen device 600, make hydrogen sulfide and the Hydrogen Separation in gaseous phase materials by the solvent doctor treatment, hydrogen sulfide imports in the sour gas of pipelines 102 and operates for recovery sulphur through pipeline 501, hydrogen imports in the hydrogen in pipelines 109 and operates for hydrofining through pipeline 509, the water material is discharged through pipeline 504, oil phase material imports air lift devulcanizer 603 through pipeline 503, in air lift devulcanizer 603, the hydrogen sulfide dissolved in oil phase material is separated and enter pipeline 500, hydrogen sulfide in pipeline 500 imports in the sour gas of pipeline 102 and operates for recovery sulphur, remaining oil phase material obtains the hydrofining product after in pipeline 505 importing fractionators 604, carrying out fractionation, and the character of this hydrofining product is as shown in table 1.
After moving three months according to the method described above, not finding has substantial obstruction and corrosion phenomenon in the pipeline of hydrofining technology, and the technique overall operation is good.Illustrate thus the present invention adopt with described hydrogenation after the Process Gas heat exchange after quenched water as the water filling of hydrotreated product, be feasible, can greatly reduce the demand of hydrofining technology to fresh water thus, and reduce the water treatment expense.
Below describe by reference to the accompanying drawings the preferred embodiment of the present invention in detail; but; the present invention is not limited to the detail in above-mentioned embodiment; in technical conceive scope of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characterictic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode, for fear of unnecessary repetition, the present invention is to the explanation no longer separately of various possible array modes.
In addition, between various embodiment of the present invention, also can carry out arbitrary combination, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (10)
1. the method for a coproduction sulphur and hydrofining product, the following steps that the method comprises successively or carries out simultaneously:
(1) under the claus reaction condition, the sour gas that will contain hydrogen sulfide contacts with oxygen-containing gas, obtains sulphur and contains SO
2claus tail gases, described Claus tail gases is carried out to hydrogenating reduction with by SO
2be converted into H
2s, obtain the Process Gas after hydrogenation, and will carry out solvent desulfurization processing after the Process Gas after described hydrogenation and quenched water heat exchange;
(2) stock oil is carried out to the hydrofining processing, obtain refined products, and described refined products is mixed with washing water to described refined products is carried out to water filling, obtain the refined products after water filling, and separate the hydrofining product from the refined products described water filling;
It is characterized in that, described washing water contain the quenched water after (1) middle heat exchange in steps.
2. method according to claim 1, wherein, described washing water are the quenched water after heat exchange in step (1).
3. method according to claim 1 and 2, wherein, with respect to the described refined products of 1 weight part, the consumption of described washing water is the 0.05-0.3 weight part.
4. method according to claim 1 and 2, wherein, in the quenched water in step (1) after heat exchange, the content of ammonia nitrogen is 200-800mg/L, and the content of element sulphur is 150-300mg/L, and the content of chlorine element is 0.001-4mg/L.
5. method according to claim 1 and 2, wherein, the temperature of described washing water is 20-50 ℃.
6. method according to claim 1 and 2, wherein, the method for extracting the hydrofining product from described mixed material comprises: the refined products after described water filling is carried out to high pressure air cooling, oily water separation, air lift desulfurization and fractionation successively.
7. method according to claim 1 and 2, wherein, described stock oil contains coking oil and straight-run diesel oil, and the weight ratio of coking oil and straight-run diesel oil is 1:5-20; Perhaps described stock oil is at least one in straight-run spirit, coker gasoline and non-aromatics.
8. method according to claim 1 and 2, wherein, in described Claus tail gases, SO
2content be 0.2-0.3 volume %.
9. method according to claim 1 and 2, wherein, in described sour gas, the content of hydrogen sulfide is 75-95 volume %.
10. method according to claim 1, wherein, the hydrogen sulfide in described sour gas partly or entirely derives from the operation of extracting the hydrofining product in step (2) from the refined products described water filling.
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| CN105947992A (en) * | 2016-06-02 | 2016-09-21 | 山东三维石化工程股份有限公司 | SWSR-8 pressurization sulfur recovery process |
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