CN105518106A - Hydrocarbon hydrotreating device and method for removing chloride from a hydrocarbon stream - Google Patents
Hydrocarbon hydrotreating device and method for removing chloride from a hydrocarbon stream Download PDFInfo
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- CN105518106A CN105518106A CN201480049553.4A CN201480049553A CN105518106A CN 105518106 A CN105518106 A CN 105518106A CN 201480049553 A CN201480049553 A CN 201480049553A CN 105518106 A CN105518106 A CN 105518106A
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- gas oil
- hydrocarbon stream
- hydrocarbon
- adsorbent bed
- tower
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 83
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 83
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 81
- 238000000034 method Methods 0.000 title claims abstract description 22
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 title claims description 25
- 239000003463 adsorbent Substances 0.000 claims abstract description 50
- 238000004939 coking Methods 0.000 claims description 22
- 239000000203 mixture Substances 0.000 claims description 15
- 239000002594 sorbent Substances 0.000 claims description 15
- 235000014121 butter Nutrition 0.000 claims description 10
- 238000006298 dechlorination reaction Methods 0.000 claims description 8
- 239000012530 fluid Substances 0.000 claims description 7
- 238000001179 sorption measurement Methods 0.000 claims description 7
- 239000005995 Aluminium silicate Substances 0.000 claims description 6
- PZZYQPZGQPZBDN-UHFFFAOYSA-N aluminium silicate Chemical compound O=[Al]O[Si](=O)O[Al]=O PZZYQPZGQPZBDN-UHFFFAOYSA-N 0.000 claims description 6
- 229910000323 aluminium silicate Inorganic materials 0.000 claims description 6
- 235000012211 aluminium silicate Nutrition 0.000 claims description 6
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 6
- 150000001805 chlorine compounds Chemical class 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 45
- 239000003921 oil Substances 0.000 description 43
- 239000010779 crude oil Substances 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 239000003208 petroleum Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 238000005336 cracking Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- DZMDPHNGKBEVRE-UHFFFAOYSA-N 1-chloroheptane Chemical compound CCCCCCCCl DZMDPHNGKBEVRE-UHFFFAOYSA-N 0.000 description 1
- KBOBQLJBYKKAPN-UHFFFAOYSA-N 2-chloro-2-methylhexane Chemical compound CCCCC(C)(C)Cl KBOBQLJBYKKAPN-UHFFFAOYSA-N 0.000 description 1
- NXXHAWKBICGUCK-UHFFFAOYSA-N 2-chloro-2-methylpentane Chemical compound CCCC(C)(C)Cl NXXHAWKBICGUCK-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 1
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000007859 condensation product Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 125000005843 halogen group Chemical group 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 150000003071 polychlorinated biphenyls Chemical class 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000009938 salting Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 230000003245 working 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
- 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
- C10G67/06—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 a sorption process 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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
- C10G25/03—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material with crystalline alumino-silicates, e.g. molecular sieves
-
- 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
- C10G2300/10—Feedstock materials
- C10G2300/1074—Vacuum distillates
-
- 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
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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)
- Crystallography & Structural Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
Abstract
A method for processing hydrocarbons includes providing a hydrocarbon stream including chlorides from one or more of a crude, vacuum or coker column and contacting the provided hydrocarbon stream with an adsorbent capable of adsorbing the chlorides from the hydrocarbon stream. The dechlorinated hydrocarbon stream is then provided to a hydrotreater reactor.
Description
Prioity claim
This application claims the sequence number submitted on August 21st, 2013 is No.13/972, the right of priority of the U.S. Patent application of 096, and its content is combined by the overall mode quoted at this.
Background technology
The increase that the change that crude oil demand amount increases has caused diesel oil and jet fuel to produce, causes refinery with their device of fractionation mode operation and the needs added for hydrotreatment.But crude oil pollution thing must in hydrotreatment pre-treatment.Especially, must alleviate and comprise organic and chloride contaminants that is butter.
Organic chloride content is not the build-in attribute of crude oil, but accidentally or unexpectedly pollutes generation by it.In other words, other physical property of the amount of the organic chloride found in crude oil and the place of crude oil extraction or crude oil is uncorrelated.Correspondingly, existing oil in test of crude can not provide the reliable expression of following chloride level.Therefore, the new crude oil selected always is considered as the excessive risk in hydrotreater with chloride contamination.
Usually, the hydrotreater had for halid removal system can be run.But this hydrotreater runs and/or safeguards expensive.Thus, their operation is impracticable.Other remission method comprising metallurgical upgrading and washing water has its widely used restricted condition of prevention.
The sampling analysis of the crude oil that some refinerys receive reflects the salts contg from 10 to 300PTB (pound every thousand barrels) (by weight, 34 to 1024/1000000ths) scope.Although there is de-salting operation, the data presentation of most refinery has a large amount of organic and butters at the side opening place of crude tower, coking tower and/or vacuum column, particularly in the light vacuum gas oil (LVGO) from vacuum column and the light coker gas oil (LCGO) from coking tower.Therefore, although relatively high at the chloride content at these towers side opening place separately, the typical chlorides restriction in most of hydrotreatment apparatus is relatively low, and the upper limit is set to 1/1000000th by weight.
Excessive muriate can cause major failures, comprises chloride stress cracking corrosion cracking (SCC).By the pipeline that selection material in hydrotreater construction process and/or reinforcement use through hydrotreater, SCC phenomenon can to a certain degree alleviated.But anti-SCC material is usually bought and is safeguarded more expensive.Correspondingly, organicly the relative lower technique of cost is needed with butter for removing from crude tower, coking tower and/or vacuum column overhead product.
Summary of the invention
One aspect of the present invention is a kind of method for the treatment of hydrocarbon/hydrocarbon polymer, and described method comprises providing and comprises muriatic hydrocarbon stream, and it is from crude tower, vacuum column and/or coking tower.By provided hydrocarbon stream with can from the adsorbent contact of the adsorbing chlorinated thing of described hydrocarbon stream.Then dechlorination hydrocarbon stream is provided to hydrotreating reactor.
Another aspect of the present invention is a kind of hydrocarbon hydrotreater, and it has: crude tower, vacuum column and/or coking tower; Adsorbent bed, it is arranged on the downstream of crude tower, vacuum column and/or coking tower and is communicated with its fluid, to make from the adsorbent contact in the hydrocarbon stream of crude tower, vacuum column and/or coking tower and adsorbent bed.Adsorbent bed can adsorbing chlorinated thing.Hydrotreating reactor is arranged on the downstream of adsorbent bed and is communicated with to process hydrocarbon stream with adsorbent bed fluid.
Accompanying drawing explanation
Drawings show an embodiment of the muriate adsorption method before entering hydrocarbon hydrotreater of the present invention.
Embodiment
Propose before hydrocarbon stream enters hydrotreating reactor, from described stream, remove organic and method that is butter.
Referring now to accompanying drawing, the hydroprocessing processes comprising muriate absorption is designated generally as 10.Thered is provided by circuit 12 by one or more in vacuum column, crude tower and coking tower containing organic and hydrocarbon stream that is butter.Hydrocarbon stream preferably include in light vacuum gas oil, heavy vacuum gas oil, heavy atmospheric gas oil, heavy coker gas oil, light coker gas oil, extremely light coker gas oil (lightlightcokergasoil), vacuum column overhead product, pressure naphtha and virgin naphtha one or more.A kind of exemplary hydrocarbon stream comprises light vacuum gas oil, heavy vacuum gas oil, heavy coker gas oil and petroleum naphtha.The hydrocarbon stream leaving tower generally has the chloride content reaching 40/1000000ths by weight.
Circuit 12 is preferably shunting/bifurcated.Reservoir circuit 14 allows described stream to use the refrigerating unit 16 of the fin fan in such as figure to cool, and is transported in reservoir (not shown) when downstream hydrotreater is in " shut " mode".Cracking circuit 18 allows described stream walk around hydrotreater and be transported to hydrocracker unit (not shown) alternatively.But in the normal operation period, hydrotreater circuit 20 transportation of hydrocarbon flows to hydrotreater.Before entering hydrotreater, the chloride content that first will reduce hydrocarbon stream is assembled to prevent the muriate in hydrotreater.
In vacuum column, crude tower and/or coking tower downstream, arrange adsorbent bed 22, it is connected to hydrotreater circuit 20.Adsorbent bed 22, containing sorbent material, is preferably chosen as and can adsorbs organic and inorganic chlorinating compounds.Preferably, the sorbent material contained in adsorbent bed 22 allows physical adsorption and/or chemisorption.The examples material used in adsorbent bed 22 comprises the sorbent material containing one or more in aluminum oxide, pure aluminium silicate and composition thereof.Especially, the sorbent material chloride cpd that can adsorb is including, but not limited to hydrochloric acid (HCl), ammonium chloride (NH
4cl), sodium-chlor (NaCl), calcium chloride (CaCl
2), magnesium chloride (MgCl
2), polychlorobiphenyl (PCBs), 1-chloroheptane, 2-chloro-2-methyl hexane and 2-chloro-2-methyl pentane.Sorbent material preferably has up to 20wt% (by weight), chloride counter ability more preferably in 10wt% to 20wt% scope.If needed, the temperature of hydrocarbon stream is preferably adjustable to strengthen adsorption efficiency.That is, the temperature of hydrocarbon stream can be controlled by adding optional heating or refrigerating unit to hydrotreatment circuit 20, has low if ambient room temperature (such as 20 DEG C) is to the temperature of 130 DEG C of scopes to make the hydrocarbon stream entering bed 22.More preferably, when hydrocarbon stream enter adsorbent bed 22 and Contact-sorption agent time, the temperature of hydrocarbon stream is 125 DEG C.Those skilled in the art will recognize that and can use other temperature for different sorbent material, and do not deviate from scope of the present invention.
Adsorbent bed 22 preferably arranges to be of a size of and provides rational working life and allow the hydrocarbon stream of enough flow rates to pass through adsorbent bed.Such as, there is 66m
3the adsorbent bed expection of volume has the work-ing life of 12 months.In addition, adsorbent bed preferably adapts to 120m
3hydrocarbon stream flow rate hourly.Those of ordinary skill in the art will appreciate that the size of catalyst bed can change adapt to different flow rate and/or have different working lives, and does not deviate from scope of the present invention.
From adsorbent bed 22 out after, the organic and butter content of hydrocarbon stream reduces widely.Preferably, 1/1000000th is less than by weight from the chloride content of adsorbent bed 22 hydrocarbon stream out.More preferably, chloride content is less than 0.1/1000000th by weight.This chloride content advantageously alleviates the SCC phenomenon caused by muriate.
Once the sorbent material in adsorbent bed 22 reaches working life, sorbent material can be replaced.The sorbent material used can regenerate, be dropped/dispose or use other ability as known in the art.
In the downstream of adsorbent bed 22, dechlorination hydrocarbon stream is provided to hydrotreater.Especially, dechlorination stream is transferred as mixing to form mixed flow 32 with the gas oil stream 26 merged preferably by circuit 24.The gas oil stream 26 merged comprises the hydrocarbon from other source, the cold feed 30 comprising hot feed 28 and use heat exchanger 31 to heat, each charging can comprise in light vacuum gas oil, heavy vacuum gas oil, heavy atmospheric gas oil, heavy coker gas oil, light coker gas oil, extremely light coker gas oil, vacuum column overhead product, pressure naphtha and virgin naphtha one or more.Heat exchanger 31 for heating cold feed 30 preferably receives the high pressure steam (HPS) as input 31a.Because HPS cools in heat exchanger 31, and flow out from heat exchanger as high pressure condensation product (HPC) 31b.Dechlorination stream in circuit 24 and the gas oil stream 26 of merging be mixed to form mixed flow 32.Then mixed flow 32 is provided to feed surge tank 36 as known in the art by one or more strainer 34.
The output of feed surge tank 36 is then by charge pump 38 and one or more pre-heaters 40 to combined feed well heater 42.Then, after the heating, then described stream be transported to reactor 44.Reactor effluent is conducted through pre-heaters 40 to provide heat to hydrocarbon stream.Pre-heaters 40 is preferably heat exchanger.Therefore, except heating enters except the stream of combined feed well heater, pre-heaters 40 also helps cooling reactor discharge.Then reactor effluent is supplied to another cooling unit 46, such as air-cooler, and is provided to high-pressure separator 48 to be separated liquid state and the gaseous parts of described stream.
The gaseous parts of hydrocarbon stream flows out from separator 48 and is provided to recycle gas washer 50 for removal impurity.Then gas through washing be transported to compressor 52, and be recycled to combined feed well heater 42 and reactor 44 as input.High-pressure separator also produces the sour water being flowed out separator 48 by circuit 49 as by product.This sour water is the waste water of the waste product containing such as hydrogen sulfide and ammonia.
The liquid part of described hydrocarbon stream flows out high-pressure separator 48 and enters stripping tower 54 with separation of liquid and gaseous composition further.Gaseous composition is removed from stripping tower 54 as tail gas 55, stripping tower liquid emission thing is transported to fractionator 56, hydrocarbon stream to be separated into various different hydrocarbon output, comprise composition 56d bottom petroleum naphtha 56a, kerosene 56b, diesel oil 56c and/or vacuum gas oil.That is, low-pressure steam enters fractionator 56 by incoming line 57, and inputs hydrocarbon stream and be divided into various composition output 56a-56d based on boiling points different separately, as known in the art.The petroleum naphtha output 56a of fractionator 56 is cooled before entering to receptor 58, and the hydrocarbon liquid exported is then separated to make a part be recycled to fractionator, and a part is output as hydrocarbon output.Sour water is removed from receptor 58 by circuit 59.
The muriatic minimizing reducing the washing water yield that permission uses in hydroprocessing processes in hydrotreater.Especially, less washing water are needed at the upstream and downstream process line of air-cooler 46.The same amount which results in the acid water yield produced during hydrotreatment reduces.
Light vacuum gas oil (LVGO) is the hydrotreatment composition being the most easily subject to chloride contamination.Correspondingly, therefore LVGO stream is the major objective of muriate absorption, as illustrated in the drawings.But, one of ordinary skilled in the art will appreciate that this muriate adsorption process except or the use that replaces it on LVGO stream be applicable to other hydrocarbon stream and do not depart from the scope of the present invention.
Specific embodiment
Although be described below in conjunction with specific embodiment, be understandable that this description is intended to illustrate and does not limit the scope of above-mentioned specification sheets and claims.
The first embodiment of the present invention is a kind of method for the treatment of hydrocarbon, and described method comprises providing and comprises muriatic hydrocarbon stream, its one or more from crude tower, vacuum column or coking tower; Thered is provided hydrocarbon stream and the muriatic adsorbent contact that can adsorb from hydrocarbon stream are provided; Dechlorination hydrocarbon stream is provided to hydrotreating reactor.One embodiment of the present of invention be until the first embodiment in this section this section in preceding embodiment one, any or all, wherein provided hydrocarbon stream comprise in light vacuum gas oil, heavy vacuum gas oil, heavy atmospheric gas oil, heavy coker gas oil, light coker gas oil, extremely light coker gas oil, vacuum column overhead product, pressure naphtha, virgin naphtha and composition thereof one or more.One embodiment of the present of invention be until the first embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream comprises light vacuum gas oil, heavy vacuum gas oil, heavy coker gas oil and petroleum naphtha.One embodiment of the present of invention be until the first embodiment in this section this section in preceding embodiment one, any or all, wherein provided hydrocarbon stream has the chloride content reaching 40/1000000ths by weight, and dechlorination stream has the chloride content by weight in the scope being less than 1/1000000th.One embodiment of the present of invention be until the first embodiment in this section this section in preceding embodiment one, any or all, wherein sorbent material comprises one or more in aluminum oxide, pure aluminium silicate and composition thereof.One embodiment of the present of invention be until the first embodiment in this section this section in preceding embodiment one, any or all, wherein contact procedure temperature that provided hydrocarbon stream is provided when be more than or equal to envrionment temperature and up to 130 DEG C between make this hydrocarbon stream and adsorbent contact.One embodiment of the present of invention be until the first embodiment in this section this section in preceding embodiment one, any or all, wherein said temperature is 125 DEG C.One embodiment of the present of invention be until the first embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream comprises organic chloride and butter.
The second embodiment of the present invention is a kind of hydrocarbon hydrotreater, and it comprises crude tower, vacuum column and/or coking tower; Adsorbent bed, it is arranged on the downstream of crude tower, vacuum column and/or coking tower and is communicated with crude tower, vacuum column and/or coking tower fluid, to make from the hydrocarbon stream of crude tower, vacuum column and/or coking tower and the adsorbent contact in adsorbent bed, described adsorbent bed can adsorbing chlorinated thing; And hydrotreating reactor, it is arranged on adsorbent bed downstream and is communicated with adsorbent bed fluid.One embodiment of the present of invention be comprise until the second embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream comprises one or more in light vacuum gas oil, heavy vacuum gas oil, heavy atmospheric gas oil, heavy coker gas oil, light coker gas oil, extremely light coker gas oil, vacuum column overhead product, pressure naphtha, virgin naphtha and composition thereof.One embodiment of the present of invention be until the second embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream comprises light vacuum gas oil, heavy vacuum gas oil, heavy coker gas oil and petroleum naphtha.One embodiment of the present of invention be until the second embodiment in this section this section in preceding embodiment one, any or all, wherein the downstream of adsorption bed merged with gas oil combined feed before entering hydrotreating reactor.One embodiment of the present of invention be until the second embodiment in this section this section in preceding embodiment one, any or all, wherein adsorbent bed has one or more the sorbent material comprised in aluminum oxide, pure aluminium silicate and its mixture.One embodiment of the present of invention be until the second embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream enters adsorbent bed up to the chloride content of 40/1000000ths by weight to have, and leaves adsorbent bed with the chloride content had by weight in the scope being less than 1/1000000th.One embodiment of the present of invention be until the second embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream be equal to or greater than ambient room temperature and up to the temperature of 130 DEG C under enter adsorbent bed.One embodiment of the present of invention be until the second embodiment in this section this section in preceding embodiment one, any or all, wherein said temperature is 125 DEG C.One embodiment of the present of invention be until the second embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream comprises organic chloride and butter.
The third embodiment of the present invention is a kind of hydrocarbon hydrotreater, and it comprises crude tower, vacuum column and/or coking tower; Adsorbent bed containing sorbent material, described sorbent material comprise in aluminum oxide, pure aluminium silicate and its mixture one or more, described adsorbent bed is arranged on the downstream of crude tower, vacuum column and/or coking tower, to make described adsorbent contact from the hydrocarbon stream of crude tower, vacuum column and/or coking tower; And hydrotreating reactor, it is arranged on adsorbent bed downstream and is communicated with adsorbent bed fluid.One embodiment of the present of invention be until the 3rd embodiment in this section this section in preceding embodiment one, any or all, wherein hydrocarbon stream comprises organic chloride and butter, and is equal to or greater than envrionment temperature in temperature and reaches between 130 DEG C and enter adsorbent bed.One embodiment of the present of invention be until the 3rd embodiment in this section this section in preceding embodiment one, any or all, wherein the downstream of adsorbent bed merged with gas oil combined feed before entering hydrotreating reactor.
Although shown at least one exemplary embodiment in aforesaid detailed description, cognoscible has been have a large amount of modification.It is also recognized that, described exemplary embodiment is only example, its scope do not limited the present invention in any way, application and structure.And aforementioned detailed description is provided for implementing exemplary embodiment of the present invention path profile easily to those skilled in the art.Be understandable that and can make various change for the layout of the element described in the exemplary embodiment and function, and do not deviate from the scope of the present invention that claims limit.
Claims (10)
1. a method for processing hydrocarbons, described method comprises:
There is provided and comprise muriatic hydrocarbon stream (12), its one or more from crude tower, vacuum column or coking tower;
Make in provided hydrocarbon stream (12) and adsorption bed (22) can from the adsorbent contact of the adsorbing chlorinated thing of hydrocarbon stream; With
The hydrocarbon stream of dechlorination is provided to hydrotreating reactor (44).
2. method according to claim 1, wherein provided hydrocarbon stream (12) comprise in light vacuum gas oil, heavy vacuum gas oil, heavy atmospheric gas oil, heavy coker gas oil, light coker gas oil, extremely light coker gas oil, vacuum column overhead product, pressure naphtha, virgin naphtha and composition thereof one or more.
3. method according to claim 1, wherein provided hydrocarbon stream (12) have by weight up to 40/1000000ths chloride content, dechlorination stream has the chloride content by weight in the scope being less than 1/1000000th.
4. method according to claim 1, wherein sorbent material comprises one or more in aluminum oxide, pure aluminium silicate and composition thereof.
5. a hydrocarbon hydrotreater, comprising:
Crude tower, vacuum column and/or coking tower;
Adsorbent bed (22), it is arranged on the downstream of described crude tower, vacuum column and/or coking tower and is communicated with described crude tower, vacuum column and/or coking tower fluid, to make from the adsorbent contact in hydrocarbon stream (12) and the described adsorbent bed of described crude tower, vacuum column and/or coking tower, described adsorbent bed can adsorbing chlorinated thing; With
Hydrotreating reactor (44), it is arranged on the downstream of described adsorbent bed and is communicated with described adsorbent bed fluid.
6. hydrocarbon hydrotreater according to claim 5, wherein said hydrocarbon stream (12) comprise in light vacuum gas oil, heavy vacuum gas oil, heavy atmospheric gas oil, heavy coker gas oil, light coker gas oil, extremely light coker gas oil, vacuum column overhead product, pressure naphtha, virgin naphtha and composition thereof one or more.
7. hydrocarbon hydrotreater according to claim 5, the downstream of wherein said adsorbent bed (22) merged with gas oil combined feed before entering described hydrotreating reactor.
8. hydrocarbon hydrotreater according to claim 5, wherein said adsorbent bed (22) has one or more the sorbent material comprised in aluminum oxide, pure aluminium silicate and composition thereof.
9. hydrocarbon hydrotreater according to claim 5, wherein hydrocarbon stream (12) be equal to or greater than ambient room temperature and up to 130 DEG C between temperature under enter described adsorbent bed (22).
10. hydrocarbon hydrotreater according to claim 5, wherein hydrocarbon stream (12) comprises organic chloride and butter.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US13/972,096 US20150053589A1 (en) | 2013-08-21 | 2013-08-21 | Hydrocarbon hydrotreating device and method for removing chloride from a hydrocarbon stream |
| US13/972,096 | 2013-08-21 | ||
| PCT/US2014/050840 WO2015026592A1 (en) | 2013-08-21 | 2014-08-13 | Hydrocarbon hydrotreating device and method for removing chloride from a hydrocarbon stream |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105518106A true CN105518106A (en) | 2016-04-20 |
Family
ID=52479403
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480049553.4A Pending CN105518106A (en) | 2013-08-21 | 2014-08-13 | Hydrocarbon hydrotreating device and method for removing chloride from a hydrocarbon stream |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20150053589A1 (en) |
| EP (1) | EP3036310A4 (en) |
| CN (1) | CN105518106A (en) |
| RU (1) | RU2016109057A (en) |
| WO (1) | WO2015026592A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114641556A (en) * | 2019-11-13 | 2022-06-17 | 托普索公司 | Halide removal scrubbing system for hydrocarbon streams |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109563414B (en) | 2016-08-01 | 2021-07-27 | 沙特基础全球技术有限公司 | Dechlorination of mixed plastic pyrolysis oils using devolatilization extrusion and chloride scavengers |
| CN109694737B (en) * | 2017-10-20 | 2021-01-05 | 中国石油化工股份有限公司 | Dechlorination method of alkylate oil |
| WO2021204821A1 (en) | 2020-04-07 | 2021-10-14 | Total Research & Technology Feluy | Purification of waste plastic based oil via first a trap and second via an hydrotreatment |
| US20220010213A1 (en) * | 2020-07-10 | 2022-01-13 | Uop Llc | Process for pvc-containing mixed plastic waste pyrolysis |
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- 2014-08-13 WO PCT/US2014/050840 patent/WO2015026592A1/en active Application Filing
- 2014-08-13 CN CN201480049553.4A patent/CN105518106A/en active Pending
- 2014-08-13 EP EP14838207.0A patent/EP3036310A4/en not_active Withdrawn
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| CN114641556B (en) * | 2019-11-13 | 2024-03-01 | 托普索公司 | Halide removal wash system for hydrocarbon streams |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2015026592A1 (en) | 2015-02-26 |
| US20150053589A1 (en) | 2015-02-26 |
| EP3036310A1 (en) | 2016-06-29 |
| EP3036310A4 (en) | 2017-03-22 |
| RU2016109057A (en) | 2017-09-18 |
| RU2016109057A3 (en) | 2018-05-22 |
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