CN209352833U - For producing the process unit of demetallated hydrocarbon from contaminated hydrocarbon - Google Patents
For producing the process unit of demetallated hydrocarbon from contaminated hydrocarbon Download PDFInfo
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- CN209352833U CN209352833U CN201821009597.6U CN201821009597U CN209352833U CN 209352833 U CN209352833 U CN 209352833U CN 201821009597 U CN201821009597 U CN 201821009597U CN 209352833 U CN209352833 U CN 209352833U
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- hydrocarbon
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- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 119
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 119
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 119
- 238000000034 method Methods 0.000 title claims abstract description 74
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 92
- 239000002253 acid Substances 0.000 claims abstract description 43
- 238000004062 sedimentation Methods 0.000 claims abstract description 43
- 239000012530 fluid Substances 0.000 claims abstract description 32
- 238000004891 communication Methods 0.000 claims abstract description 30
- 238000001704 evaporation Methods 0.000 claims abstract description 24
- 230000008020 evaporation Effects 0.000 claims abstract description 22
- 238000004064 recycling Methods 0.000 claims abstract description 13
- 239000012267 brine Substances 0.000 claims abstract description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 29
- 239000007789 gas Substances 0.000 claims description 17
- 229910052739 hydrogen Inorganic materials 0.000 claims description 14
- 239000001257 hydrogen Substances 0.000 claims description 13
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 12
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 7
- 239000010931 gold Substances 0.000 claims description 5
- 229910052737 gold Inorganic materials 0.000 claims description 5
- 238000005194 fractionation Methods 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 2
- 239000012071 phase Substances 0.000 description 55
- 239000011269 tar Substances 0.000 description 44
- 229910052751 metal Inorganic materials 0.000 description 28
- 239000002184 metal Substances 0.000 description 28
- 239000000203 mixture Substances 0.000 description 26
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 15
- 239000003921 oil Substances 0.000 description 14
- 238000005984 hydrogenation reaction Methods 0.000 description 13
- 238000005554 pickling Methods 0.000 description 13
- 239000000463 material Substances 0.000 description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 239000011260 aqueous acid Substances 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- 229910052760 oxygen Inorganic materials 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 238000002309 gasification Methods 0.000 description 7
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 239000000571 coke Substances 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 238000011143 downstream manufacturing Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 230000003068 static effect Effects 0.000 description 4
- 150000007513 acids Chemical class 0.000 description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 3
- 125000005842 heteroatom Chemical group 0.000 description 3
- 230000016507 interphase Effects 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000001376 precipitating effect Effects 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 239000010802 sludge Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- -1 sulphur Compound Chemical class 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- WURBVZBTWMNKQT-UHFFFAOYSA-N 1-(4-chlorophenoxy)-3,3-dimethyl-1-(1,2,4-triazol-1-yl)butan-2-one Chemical compound C1=NC=NN1C(C(=O)C(C)(C)C)OC1=CC=C(Cl)C=C1 WURBVZBTWMNKQT-UHFFFAOYSA-N 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- 244000025254 Cannabis sativa Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 239000012223 aqueous fraction Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000012075 bio-oil Substances 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000004820 halides Chemical class 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 150000007522 mineralic acids Chemical class 0.000 description 1
- 150000004780 naphthols Chemical class 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 125000004433 nitrogen atom Chemical group N* 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 125000000962 organic group Chemical group 0.000 description 1
- 125000001477 organic nitrogen group Chemical group 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 150000007965 phenolic acids Chemical class 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000004448 titration Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/10—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one acid-treatment step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G17/00—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge
- C10G17/02—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acids or acid-containing liquids, e.g. acid sludge
- C10G17/04—Liquid-liquid treatment forming two immiscible phases
- C10G17/06—Liquid-liquid treatment forming two immiscible phases using acids derived from sulfur or acid sludge thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/08—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by treating with water
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including acid treatment as the refining step in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4081—Recycling aspects
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
This disclosure relates to the process unit for producing demetallated hydrocarbon from contaminated hydrocarbon, comprising: for mixed device, with the one or more entrances for contaminated hydrocarbon entrance and with sour entrance being fluid communication, and with outlet；Sedimentation basin, it is with entrance, water phase outlet is mutually exported with the first hydrocarbon, device for evaporation and concentration, it is with entrance, water out and brine outlet, wherein the entrance of the outlet for mixed device and the sedimentation basin is to be in fluid communication, and it is characterized in that the water phase outlet of the entrance and the sedimentation basin of the device for evaporation and concentration is to be in fluid communication, the water out of the device for evaporation and concentration and sour entrance are to be in fluid communication, the hydrocarbon, which mutually exports, provides demetallated hydrocarbon for recycling, the associated benefits that there is such process unit water consumption to reduce, namely acid charging can be concentrated acid, and it is diluted by the water recycled from the device for evaporation and concentration.
Description
Technical field
This application involves the process units and method for producing demetallated hydrocarbon from contaminated hydrocarbon.
Background technique
In the processing of hydrocarbon mixture, heteroatomic removal is the weight that product is up to specification and environment or operation is avoided to challenge
Want step.Hydrogenation treatment is by mixing hetero atom (such as sulphur, nitrogen and oxygen) them from contaminated hydrocarbon and reaction with hydrogen
The conventional route of object recycling.However, if there is metal pollutant, even if concentration is relatively low, the activity of catalyst also can be by
It seriously affects.Metal pollutant may cause the solid product formed on catalytic surfaces, and such as coke or glue, having makes at hydrogenation
Manage the influence of catalyst inactivation.Therefore, in the hydrotreating of the charging with tenor, in the upper of hydrotreatment step
Trip, so-called guard bed is necessary.Tar is a kind of source of the high hydrocarbon mixture of metal amount.When metal bonding is in coke
When in structure present in oil, it has therefore been surprisingly found that can be released by contacting contaminated hydrocarbon mixture with aqueous acid
The metal of amplification quantity.It has also been found that can be with the process unit of configuration integration, wherein by the by-product in gas cleaning processes step
Sulfuric acid is produced, can be used in pickling demetal process.However, a large amount of acid of pickling consumption or water, relate to it is therefore desirable for reducing
And the consumption of the water of pickling.
Utility model content
According to the present invention it has been found that the combination of sedimentation basin and two centrifuges provides pole when implementing the pickling of tar
Property acid mutually and the optimal separation of non-polar hydrocarbon phase, and optimally realized from from the spent acid of pickling by evaporative precipitation
Except metal.
" acid value " is the instruction of the organic acidity of stream.Acid value is defined as the amount of specific alkali by ASTM D664, with every gram of sample
The milligram number of product potassium hydroxide indicates, needs using the sample in particular detection system titration specific solvent to specific terminal.
If concentration is with ppmwStatement, this is construed as million/weight number.
According to the use of term in refinery practice field, " hydrocarbon mixture " or " contaminated hydrocarbon mixture " should include master
It to include any stream of the other elements (such as oxygen, sulphur, nitrogen, halide and metal) except hydrogen and carbon for hydrocarbon but also.
As used in text, " gasification " should be understood such technique: wherein just be oxidized to CO in shortage oxygen or presence2
For sub- stoichiometric amount oxygen under heating carbonaceous charging (such as coal or biomass).Such technique is also referred to as other
Term, such as " pyrolysis " or " coke production ".The product of gasification generally includes solid phase, gas phase and liquid phase, i.e. tar.For letter
Just, term " gasification " will be used to cover all such techniques, unless otherwise stated.
As used in text, according to the term of this field, " contaminated hydrocarbon " or " tar " should be understood to be originated from such
The derivative of the hydrocarbonaceous liquid of gasification process or such liquid is alternatively referred to as term " light oil ", " carbolic oil (carbolic
Oil) ", " naphtalene oil ", " washing oil ", " carbolineum " or " pitch ".Such as " pyrolysis oil ", " bio oil ", " coal tar " and " coke-oven tar "
Term can serve to indicate that provide tar technique.For purposes of this application, " tar " be usually be pyrolyzed, coke production or
The product of coal gasification, and the term and term " contaminated hydrocarbon " exchange.Tar is characterized in hetero atom (especially nitrogen, sulphur
And oxygen) a large amount of presence and high-content aromatic hydrocarbon.The canonical parameter of tar include hydrocarbonaceous liquid be comprising 0.5% or 1% to
5%, 6% or 10% oxygen and the hydrocarbon mixture with the hydrogen content lower than 10%w/w.In general, the acid value of tar be higher than 2 or 4 and
Lower than 7 or 8mg KOH/g, density are higher than 0.90g/ml, are higher than 0.96g/ml or are higher than 1.05g/ml, and nitrogen-atoms and sulphur original
The ratio (N:S) of son is higher than 1:1,2:1,5:1 or 10:1.
As used in text, term " device for evaporation and concentration " should be used to cover one or more equipment, wherein molten
The aqueous solution of solution material is heated, and is concentrated by evaporating water, obtains purifying from the equipment by the condensation of the water of evaporation
Water flow, and from the equipment recycling the increased salt water of dissolved material concentration liquid flow.The technique alsos relate to or is not related to
The precipitating of dissolved material, and term salt water only should be understood that and refer to the increased waterborne liquid of dissolved material concentration, and not
It should imply any information of the property about dissolved material." device for evaporation and concentration " may include more than one evaporator
And condenser, such as two or three concatenated evaporator/condensers.
Broadly, this disclosure relates to be used to produce the process unit of demetallated hydrocarbon from contaminated hydrocarbon, comprising: be used for
Mixed device, with the one or more entrances for contaminated hydrocarbon entrance and with sour entrance being fluid communication, and
With outlet；Sedimentation basin is mutually exported with entrance, water phase outlet with the first hydrocarbon；For the device of evaporation and concentration, have into
Mouth, water out and brine outlet, wherein the exporting with the entrance of the sedimentation basin to be in fluid communication for mixed device,
And it is characterized in that the water phase outlet of the entrance and the sedimentation basin of the device for being used for evaporation and concentration is fluid communication, institute
The water out and sour entrance for stating the device for evaporation and concentration is are in fluid communication, and the hydrocarbon mutually exports the demetallated hydrocarbon of offer and uses
In recycling, the associated benefits of such process unit are water consumption reductions, that is, acid charging can be concentrated acid, and by from
In the water dilution that the device of evaporation and concentration recycles.
In a further embodiment, process unit further includes the first centrifuge, is gone out with entrance, hydrocarbon outlet and water
Mouthful, wherein the outlet of the entrance of first centrifuge and the sedimentation basin is to be in fluid communication, and from first centrifuge
Hydrocarbon outlet recycle the demetallated hydrocarbon, and replace the water phase outlet of the sedimentation basin or other than it, it is described to be used for
The water out of the entrance of the device of evaporation and concentration and first centrifuge is to be in fluid communication, the correlation benefit of such process unit
There is provided the increases of the purity of at least one of water phase and demetallated hydrocarbon at place, or optionally, allow in sedimentation basin less
It is totally separated from.It reduces the water in hydrocarbon phase and decreases the amount of metal being imported into downstream hydrogenation treatment process, therefore increase
Service life of catalyst.Reduce water phase in hydrocarbon amount reduce process yield loss, and reduce hydrocarbon to Environment release can
It can property.
In a further embodiment, the sedimentation basin also has the outlet of the second hydrocarbon, and wherein process unit also wraps
The second centrifuge is included, with entrance, hydrocarbon outlet and water out, wherein the entrance of second centrifuge and the sedimentation basin
Entrance from first centrifuge is that the different outlet in outlet being in fluid communication is fluid communication, and wherein from described second
The second demetallated hydrocarbon of hydrocarbon outlet recycling of centrifuge, and instead of the outlet of the water phase of the sedimentation basin or other than it, institute
The water out of the entrance and second centrifuge of stating the device for evaporation and concentration is fluid communication, such process unit
Associated benefits are suitable for the fraction in a centrifuge with density lower than water and have density high in another centrifuge
In the separation of the complicated blended tars of the fraction of water.The second demetallated hydrocarbon can individually handle or two kinds of de- gold
The hydrocarbon of category can be combined merging treatment.
In a further embodiment, during one or both of first centrifuge and second centrifuge further include
Between stream export, be fluid communication, phase with one of the entrance of the sedimentation basin or the entrance for mixed device
Pass benefit, which is that phases were separated, to be maximized, therefore minimizes the contaminated water for being oriented to downstream process.
In a further embodiment, first centrifuge or second centrifuge is extremely (if present)
A few water out and first hydrocarbon mutually export as fluid communication, associated benefits be avoid due to being recycled to sedimentation basin and
Caused additional technique volume, as long as the water of guiding downstream process is sufficiently low, and for downstream process, water phase is sufficiently pure.
In a further embodiment, one or both of first centrifuge and second centrifuge further include slurry
Stream outlet, associated benefits are the particulate matters that can be removed from the suspension sedimentation or release that feed from tar.
In a further embodiment, process unit further includes the device for hydrotreating, is gone out with entrance, hydrocarbon
Mouth and gas vent, wherein the entrance of the device for hydrotreating mutually exports with hydrogen source and first hydrocarbon, is described
The outlet of first centrifuge hydrocarbon and optional the second centrifuge hydrocarbon outlet is are in fluid communication, from the dress for hydrotreating
Hydrotreated hydrocarbon is recycled in the hydrocarbon outlet set, and recycles acid gas from the gas vent, and is optionally purified and as described
A part recycling of hydrogen source, the associated benefits of such process unit are that hydrogen and other process equipments are efficiently used and provide
Hydrotreated hydrocarbon.
In a further embodiment, process unit further includes gas fractionation unit, with entrance, hydrogen outlet and sulphur
Compound outlet；Sulfuric acid apparatus is exported with sulfide gas entrance and sulfuric acid, wherein the sulfuric acid apparatus sulfide gas enters
The sulfide outlet of mouth and gas fractionation unit is fluid communication, and the sour entrance of the sedimentation basin is with sulfuric acid outlet
It is in fluid communication, the associated benefits of such process unit are to provide at least a certain amount of sulfuric acid for pickling.
Another aspect of the present disclosure is related to for producing hydrogenation treatment from the contaminated hydrocarbon mixture for deriving from gasification process
Hydrocarbon method comprising following steps:
A. simultaneously by the contaminated hydrocarbon mixture and aqueous acid and hydration, mixture is formed,
B. the mixture is mixed after the reaction time,
C., the mixture is separated into the hydrocarbon phase of contaminated water phase and purifying by Gravity Separation,
D. the contaminated water phase is purified by evaporating, and condenses pure water to be recycled into step a,
E. optionally, at least one of the contaminated water phase and the hydrocarbon phase are purified by being centrifugated,
F. and optionally, the hydrocarbon phase of the purifying is merged with the gas rich in hydrogen, forms hydrotreating stream, and
The hydrotreating stream is oriented to hydrotreating step, forms hydrotreated hydrocarbon.
The associated benefits of such method are that this method is effective demetalization and hydrotreating method, supplement addition
The demand of water minimizes.
In a further embodiment, contaminated hydrocarbon mixture includes 0.5% or 1% to 5%, 6% or 10% oxygen,
The associated benefits of such method are that this method is effective demetalization and hydrotreating method, can be removed from hydrocarbon mixture
Oxygen.
In a further embodiment, aqueous acid is selected from the group including strong inorganic acid or organic acid, optimization citric acid, grass
Acid, hydrochloric acid, phosphoric acid, phosphoric acid or sulfuric acid, the associated benefits of such acid are effectively demetalizations.
In a further embodiment, the method does not include C, H, O, N and S that addition is higher than 0.1% comprising concentration
Except element waterborne liquid, the associated benefits of such method be avoid adding must be driven off before hydrotreating at
Point.
In a further embodiment, the concentration of aqueous acid is from 1% or 2% to 5%, 10% or 30%.
The associated benefits of such acid are metal effectively to be discharged from hydrocarbon, while minimize the demand to material.
In a further embodiment, contaminated hydrocarbon mixture and acid ratio be 50:1,20:1 or 10:1 to 2:1,
1:1 or 1:2, the associated benefits of such ratio are the volume minimizations for maximizing the release of metal, while making acid used.
In a further embodiment, the temperature in step b is 20 DEG C to 100 DEG C, the associated benefits of the temperature range
It is effectively demetalization, while does not need excessive material quality.
In a further embodiment, what this method further included the steps that step (a) upstream makes carbonaceous material gasify, with
The hydrocarbon that acid value is higher than 1.5mg KOH/g is formed, the associated benefits of such method are to provide high quality hydrocarbon by carbonaceous material.
It is important processing step from contaminated hydrocarbon mixture removal metal, because the presence of metal may be filled in refining
Cause big problem in setting.Specifically, it may be expensive for capturing the guard bed of metal, and when metal is captured on material
When, there may be high pressure drop.Therefore, the technique that chelated mineral can still not recycle them in process is desired.
Addition acid is known to remove metal from contaminated hydrocarbon mixture, however, it has been found that removal is usually in neutrality
Or close to being most effective under conditions of neutral, so that the acidification of product is avoided, because this will lead to the risk of equipment corrosion, this
Outside, most of refining product has the specification of limitation acid value.However, tar usually has the phenolic acid, carboxylic acid and cycloalkanes of high-content
Acid, therefore these products are handled in the equipment made of corrosion-resistant material.Therefore, by contacting with aqueous acid to remove gold
The pre-treatment step for belonging to pollutant will not significantly change the machinability of product, or change reactor, container and other equipment
Selection to building material, because the charging for acid value higher than 0.5mg KOH/g will consider corrosivity in refining art,
And charging of the acid value higher than 1.0,1.5 or 2.0mg KOH/g is considered corrosive, and in technological design and/or material
The concern especially and concentrated is needed in material selection.
During hydrogenation treatment, as acid compound (such as aphthenic acids, phenol, naphthols) is converted into hydrocarbon and water, acid value/acid
Property is lowered/eliminates, and hydrogenation process also has tolerance for the presence of the dissolution water of moderate.
In coke-oven tar and pyrolysis oil, the amount of metal usually can be 200-500ppmw, and in renewable source
In fat and oil, amount can also be in hundreds of ppmwLevel.Major part in these metals be in the form of soluble compounds, or
It is combined into complex compound with organic compound, can not be removed by mechanical filter, but some is also used as being suspended in coke
Particle in oil and exist or be present in the particle.
Without wishing to be bound by theory, it is believed that add acid to the release of contaminated hydrocarbon mixture as with phenol or its
The complex compound of his organic group (such as aphthenic acids) and existing metal, then recycle metal and chelating with acid.
The associated benefits of pickling demetal process are total nitrogen compound and basic nitrogen chemical combination in contaminated hydrocarbon mixture
The content of object is lowered, and thereby reduces NH3With organic nitrogen to hydrogenation treatment, especially to the inhibition of hydrocracking catalyst.
Which imply the reduction of required catalyst volume and lower hydrogen consumptions.
The selection of acid for tar pickling depends on many aspects.One importance certainly removes the energy of metal
Power is related to the sequestering power of acid and the intensity of acid.In addition, the compatibility of acid and downstream refinery practice is also important.With regard to this
Aspect, sulfuric acid have benefit, because keeping any sulfuric acid being entrained in hydrocarbon and bisulfate ion and sulfate anion under
It is easy to remove in the hydrodesulphurisation processes of trip, while removing organic sulfur and hydrogen sulfide.Similarly, organic acid also will be with downstream work
Skill is compatible, and phosphoric acid or hydrochloric acid may be further aggravated the toxic effect of phosphorus and chlorine, or even with being otherwise not present in
Element pollution downstream process in hydrocarbon charging.
In the processing of tar, the viscosity of tar is also important.Some tar are highly viscous, and can be benefited
It is handled at 50 to 100 DEG C of Yu Yue of raised temperature, and the possible viscosity of other tar is lower, therefore being at a lower temperature can
Processing.
It must also consider that feed conditions carry out design technology.If tar is derived directly from upstream pyrolysis or gasification, tar is very
It may must be cooled, to use the processing of the liquid phase of aqueous acid, and wherein from the technique of storage and processing tar, tar possibility
It must be heated, so that it is processable.
When purifying tar by pickling, the acid of the metal comprising tar can be separated from hydrocarbon phase in sedimentation basin.This
The pond operation of sample is cheap, but separates bad.
It is alternatively possible to carry out separating acid/hydrocarbon mixture by using centrifuge, but especially if by tar separation Cheng Mi
For the phase and density that degree is higher than water lower than the phase of water, this may be complicated technique.
It has been discovered, however, that by sedimentation basin and centrifuge combination be it is beneficial because segregative stream can directly from
Sedimentation basin recycling, and be less susceptible to isolated stream in sedimentation basin and can further be separated in centrifuge, therefore limitation
The number and/or size of centrifuge, such as by being centrifuged heavy hydrocarbon streams and water flow respectively, but it is not centrifuged lightweight hydrocarbon stream.In addition,
Fraction rich in particulate matter can also be recycled from one or two centrifuge, and intermediate stream can be recycled to precipitating
Pond, for further separating.
It will be from sedimentation basin and also weak acid from the water phase that one or two centrifuge used recycles, the gold with a large amount
Belong to and possible other impurities.For environment and economic cause, recycle as much as possible the stream be it is beneficial, therefore, gold
It is desired for belonging to the method for salt recycling.It is known that washing water or washing acid containing metal salt are carrying out metal by adjusting pH
After the alkali precipitation of salt, it can be recycled.However, this for the application the case where for be infeasible method, because of pH
Adjusting would generally be related to adding aqueous slkali, such as sodium hydroxide, and the amount that will lead to sodium in water phase increases.Sodium is well known catalysis
A small amount of sodium will lead to the significant shortening of catalyst life in agent poisonous substance, or even the hydrocarbon of importing downstream hydrogenation processing unit.
Instead, it was found that precipitating is beneficial at least through being concentrated by evaporation.Therefore, configured with for being concentrated by evaporation
The process unit of device (such as evaporator and condenser for Recovery and recycle water of combination) will be beneficial.In this way
Evaporator can be concatenated one or more unit, and water condenser or water condensation can be provided for each evaporator
Device can be the individual unit for all evaporators.
The hydrocarbon of purifying recycled from one or two centrifuge can then be hydrogenated processing, can individually handle or with
Density be respectively lower than water two hydrocarbon fractions and density be higher than water fraction combined treatment.Hydrotreating can be related to hydrogenation cracking
With the one or both in hydrogenation treatment.
Rich hydrogen sulfide containing stream can be recycled from the hydrogenation treatment of hydrocarbon.It can be for example by wet process sulfur process by the material
The circulation chemical conversion concentrated sulfuric acid, is used for acid cleaning process.
Detailed description of the invention
Fig. 1 shows the process layout corresponding to the disclosure.
Fig. 2 shows the process layout corresponding to the prior art.
In figure, the following drawings label refers to:
102 contaminated hydrocarbon mixtures
104 water
106 concentrated acids
108 aqueous acids
110 are used for mixed device
112 acid/hydrocarbon mixture
114 sedimentation basins
116 interphases
118 lightweight phases
120 heavy phases
122 first centrifuges
124 second centrifuges
126,130 contaminated water phases
128 mixed tar light oils and water phase
132 mixed heavy tars and water phase
The hydrocarbon phase of 134 heavys purifying
136 tar sludge
138 combined evaporators and condenser
140 strong brines
142 water
144 steam
146 condensates
202 hydrocarbon mixtures
208 aqueous acids
210 mixing reactors
214 sedimentation basins
216 contaminated water phases
The clean tar phase of 218 lightweights
The tar phase of 220 heavys purifying
Specific embodiment
Fig. 1 shows the embodiment of the technique according to the disclosure.It will be contaminated comprising oxygenatedchemicals and metal
Hydrocarbon mixture 102 optionally heats, and mixes with the aqueous acid 108 made of water 104,142 and concentrated acid 106, and be oriented to use
In mixed device, such as static mixer 110 or stirring pool, it is mixed wherein.Acid/hydrocarbon mixture 112 is oriented to
Sedimentation basin 114 is implemented mutually to separate wherein by simple gravitational settling.In the embodiment depicted in fig. 1, from sedimentation basin
Recycle 3 phases；Interphase 116, predominantly contaminated water；Lightweight phase 118 is essentially only hydrocarbon, and does not need into one
The mutually separation of step；And heavy phase 120, predominantly hydrocarbon, but contain a certain amount of contaminated water.In optional embodiment
In, single hydrocarbon phase can be only recycled, can have higher than water or lower than the density of water.By first centrifugation of the guiding of interphase 116
Machine 122, and heavy phase 120 is oriented to the second centrifuge 124.First centrifuge 122 by the stream of contaminated water phase 126 with
A certain amount of mixed tar light oil and water phase 128 separate.Mixed tar light oil and water phase 128 is directed at static mixer
110 inlet merges with other streams.Second centrifuge 124 is by the stream of contaminated water phase 130 and a small amount of mixing
Heavy tar and water phase 132, optional clean heavy tar 134 and tar sludge 136 separate.By mixed tar light oil
The entrance of static mixer 106 is oriented to water phase 128 and mixed heavy tar and water phase 132, but can also be mixed by two
The entrance of the stream guiding sedimentation basin 114 of conjunction.Two contaminated water phase streams 126 and 130 are all directed to the evaporator of combination
With condenser 138, pass through evaporation production strong brine 140 wherein.Pure water 142 is condensed, and is oriented to static mixing as charging
Device 110.By condensation and other sources, (the usually such as process steam 144 from hydrotreater is used as condensate
146 return to hydrotreater) energy for being used for evaporator is provided, but other heat sources except process steam are also possible
's.The hydrocarbon phase 134 of the hydrocarbon phase 118 of lightweight purifying and heavy purifying is oriented to hydrotreater respectively or in combination, it can be with
It is for the hydrogenation cracking device by tar conversion at lighter product, or for removing nonmetallic other hetero atom
The hydrogen treating device of (such as sulphur and nitrogen) and de- aromatic hydrocarbon and other hydrogenation process.
In a further embodiment, it is convenient to omit one or two centrifuge, because the water of moderate can be led
To hydrotreating, the residence time without serious negative effect, but in sedimentation basin may must increase in this case
Add, and must also consider the metal ladings on hydrotreating catalyst.For practical reasons, can be operated in parallel multiple centrifugations
Machine, to provide the necessary flowing of centrifuge charging.
In a further embodiment, by adding the one or both in stream 128 and 132 to stream 118, and will
Combined stream is oriented to hydrotreating, the water of moderate can be oriented to hydrotreating.
Another embodiment further relates to mutually remove a certain amount of water from light hydrocarbon by using other centrifuge.For spy
Fixed charging, it may be necessary to such embodiment, alternatively, such embodiment allows the residence time in sedimentation basin to subtract
It is few.
In alternative embodiments, single hydrocarbon phase is only recycled from sedimentation basin.Depending on the property of contaminated hydrocarbon, this
It can be light hydrocarbon or heavy hydrocarbon.
In Fig. 2, it is shown that similar technique according to prior art.Contaminated hydrocarbon comprising oxygenatedchemicals and metal
Mixture 202 is directed to the mixer-settler type equipment with mixing pit 210 with aqueous acid 208 together, occurs wherein mixed
It closes.By the sedimentation basin 214 of mixture guiding connection.From the clean tar phase 218 of settler recycling lightweight, contaminated water phase
216 and heavy purifying tar phase 220.Due to metal concentration height, contaminated water phase 216 cannot be recycled to pickling work
Skill.Metal can be by being recycled with sodium hydroxide pellets, but aqueous solutes will mutually not be suitable for being recycled to pickling, because
It can be transferred to hydrocarbon phase for a certain amount of sodium, and the hydrotreating catalyst in downstream is made to be poisoned.
Embodiment
Hydrocarbon is further purified by being related to the pickling of sedimentation basin to the demetallated technique of coke-oven tar and with centrifugation is passed through
The similar pickling for being related to sedimentation basin of product compares.
According to Fig. 1 design technology, the tar of 162 tons/h is received.By 93% sulfuric acid of tar and 2.7 tons/h, 6.5 tons/h
The recycling for supplementing water and 44.9 tons/h is hydrated simultaneously.The sludge of 4.5 tons/h, the salt water of 4 tons/h, 53 tons/h are recycled from the technique
Lightweight purifying hydrocarbon and 106 tons/h heavy purifying hydrocarbon.Evaporation technology consumes the low-pressure steam of 10 tons/h.
If contaminated water phase is not evaporated concentration, the water of 44.9 tons additional/h must be added to technique, because
Be not suitable for recycling for contaminated water phase.
Claims (8)
1. a kind of for producing the process unit of demetallated hydrocarbon from contaminated hydrocarbon, comprising:
For mixed device, has with contaminated hydrocarbon entrance and enter with one or more that sour entrance be fluid communication
Mouthful, and there is outlet,
Sedimentation basin is mutually exported with entrance, water phase outlet with the first hydrocarbon,
For the device of evaporation and concentration, with entrance, water out and brine outlet,
Wherein the exporting with the entrance of the sedimentation basin to be in fluid communication for mixed device, and it is characterized by:
The entrance of the device for evaporation and concentration and the water phase of the sedimentation basin export to be in fluid communication, and
The water out of the device for evaporation and concentration and sour entrance are to be in fluid communication, and first hydrocarbon mutually exports the de- gold of offer
The hydrocarbon of category is for recycling.
2. process unit according to claim 1, wherein the process unit further include:
First centrifuge, with entrance, hydrocarbon exports and water out,
Wherein the outlet of the entrance of first centrifuge and the sedimentation basin is fluid communication, and
Recycle the demetallated hydrocarbon from the outlet of the hydrocarbon of first centrifuge, and replace the sedimentation basin water phase outlet or
Other than it, the entrance of the device for evaporation and concentration and the water out of first centrifuge are to be in fluid communication.
3. process unit according to claim 2, wherein the sedimentation basin also has the outlet of the second hydrocarbon, and wherein technique
Device further include:
Second centrifuge, with entrance, hydrocarbon exports and water out,
Wherein the entrance of second centrifuge and the sedimentation basin be fluid communication with the entrance of first centrifuge
Different outlets is exported to be in fluid communication, and
The second demetallated hydrocarbon of recycling wherein is exported from the hydrocarbon of second centrifuge, and the water phase of the sedimentation basin is replaced to go out
Mouthful or other than it, it is described for evaporation and concentration device entrance and second centrifuge water out be fluid connect
It is logical.
4. process unit according to claim 3, wherein one of first centrifuge and second centrifuge or two
Person further includes intermediate stream outlet, is fluid with one of the entrance of the sedimentation basin or the entrance for mixed device
Connection.
5. process unit according to claim 3, wherein first centrifuge or if present described second from
At least one water out of scheming mutually exports to be in fluid communication with first hydrocarbon.
6. process unit according to claim 3, wherein one of first centrifuge and second centrifuge or two
Person further includes slurry outflux.
7. process unit according to claim 3, wherein the process unit further includes
For the device of hydrotreating, with entrance, hydrocarbon exports and gas vent,
Wherein the entrance of the device for hydrotreating mutually exported with hydrogen source and first hydrocarbon, first centrifuge
At least one of hydrocarbon outlet and optional the second centrifuge hydrocarbon outlet are to be in fluid communication,
Hydrotreated hydrocarbon is recycled from the outlet of the hydrocarbon of the device for hydrotreating,
Acid gas is recycled from the gas vent, and is optionally purified and is recycled as a part of of the hydrogen source.
8. process unit according to claim 7, wherein the process unit further includes
Gas fractionation unit is exported with entrance, hydrogen outlet and sulfide,
Sulfuric acid apparatus is exported with sulfide gas entrance and sulfuric acid,
Wherein the outlet of the sulfide of the sulfuric acid apparatus sulfide gas entrance and gas fractionation unit is is in fluid communication, and institute
Sour entrance and the sulfuric acid outlet of sedimentation basin are stated to be in fluid communication.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
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| DKPA201700395 | 2017-06-30 | ||
| DKPA201700395 | 2017-06-30 |
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| CN209352833U true CN209352833U (en) | 2019-09-06 |
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| CN201810686058.4A Pending CN109207198A (en) | 2017-06-30 | 2018-06-28 | The demetalization of hydrocarbon |
| CN201821009597.6U Active CN209352833U (en) | 2017-06-30 | 2018-06-28 | For producing the process unit of demetallated hydrocarbon from contaminated hydrocarbon |
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|---|---|
| CN (2) | CN109207198A (en) |
| AU (1) | AU2018291824B2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US2520407A (en) * | 1948-11-27 | 1950-08-29 | Sun Oil Co | Removal of inorganic matter from petroleum residua |
| US3622505A (en) * | 1969-12-24 | 1971-11-23 | Union Oil Co | Demetallization of residual oils with polyphosphoric acids |
| CN1202208C (en) * | 2003-06-03 | 2005-05-18 | 克拉玛依市金山石油化工有限公司 | Hydrocarbon oil demetalizing cycle method |
| US10752842B2 (en) * | 2015-07-02 | 2020-08-25 | Haldor Topsøe A/S | Demetallization of hydrocarbons |
| KR102341007B1 (en) * | 2015-08-21 | 2021-12-17 | 에스케이이노베이션 주식회사 | Method for removing metals from hydrocarbon oil |
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| AU2018291824B2 (en) | 2024-03-14 |
| WO2019002028A1 (en) | 2019-01-03 |
| CN109207198A (en) | 2019-01-15 |
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