CN100445243C - Method for producing benzene arenes from coarse benzene - Google Patents
Method for producing benzene arenes from coarse benzene Download PDFInfo
- Publication number
- CN100445243C CN100445243C CNB2006101368571A CN200610136857A CN100445243C CN 100445243 C CN100445243 C CN 100445243C CN B2006101368571 A CNB2006101368571 A CN B2006101368571A CN 200610136857 A CN200610136857 A CN 200610136857A CN 100445243 C CN100445243 C CN 100445243C
- Authority
- CN
- China
- Prior art keywords
- oil
- benzene
- raw material
- crude benzol
- atmosphere
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- UHOVQNZJYSORNB-UHFFFAOYSA-N monobenzene Natural products C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 147
- -1 benzene arenes Chemical class 0.000 title claims description 7
- 238000004519 manufacturing process Methods 0.000 title abstract description 4
- 241001120493 Arene Species 0.000 title 1
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 63
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000008096 xylene Substances 0.000 claims abstract description 12
- 239000002994 raw material Substances 0.000 claims description 39
- 238000000034 method Methods 0.000 claims description 33
- 238000005984 hydrogenation reaction Methods 0.000 claims description 29
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 239000003054 catalyst Substances 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 13
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 238000004821 distillation Methods 0.000 claims description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- AXFKVYBBROZOGA-UHFFFAOYSA-N [P].[Mo].[Co] Chemical class [P].[Mo].[Co] AXFKVYBBROZOGA-UHFFFAOYSA-N 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 238000005194 fractionation Methods 0.000 claims description 4
- 238000000638 solvent extraction Methods 0.000 claims description 4
- 241000282326 Felis catus Species 0.000 claims description 3
- AFTDTIZUABOECB-UHFFFAOYSA-N [Co].[Mo] Chemical class [Co].[Mo] AFTDTIZUABOECB-UHFFFAOYSA-N 0.000 claims description 2
- VKKISSAOCQRXBO-UHFFFAOYSA-N [P].[W].[Mo].[Ni] Chemical group [P].[W].[Mo].[Ni] VKKISSAOCQRXBO-UHFFFAOYSA-N 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims description 2
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 claims description 2
- 239000002904 solvent Substances 0.000 abstract description 6
- 239000003921 oil Substances 0.000 description 50
- 239000000047 product Substances 0.000 description 15
- 230000008569 process Effects 0.000 description 11
- 239000000126 substance Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000004939 coking Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 238000006116 polymerization reaction Methods 0.000 description 4
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000000895 extractive distillation Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- HUMNYLRZRPPJDN-UHFFFAOYSA-N benzaldehyde Chemical compound O=CC1=CC=CC=C1 HUMNYLRZRPPJDN-UHFFFAOYSA-N 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- PQNFLJBBNBOBRQ-UHFFFAOYSA-N indane Chemical compound C1=CC=C2CCCC2=C1 PQNFLJBBNBOBRQ-UHFFFAOYSA-N 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- LCEDQNDDFOCWGG-UHFFFAOYSA-N morpholine-4-carbaldehyde Chemical compound O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 description 2
- 238000006396 nitration reaction Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- UWHCKJMYHZGTIT-UHFFFAOYSA-N tetraethylene glycol Chemical compound OCCOCCOCCOCCO UWHCKJMYHZGTIT-UHFFFAOYSA-N 0.000 description 2
- PRBXPAHXMGDVNQ-UHFFFAOYSA-N 2-[2-(2-hydroxyethoxy)ethoxy]acetic acid Chemical compound OCCOCCOCC(O)=O PRBXPAHXMGDVNQ-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- PMVSDNDAUGGCCE-TYYBGVCCSA-L Ferrous fumarate Chemical compound [Fe+2].[O-]C(=O)\C=C\C([O-])=O PMVSDNDAUGGCCE-TYYBGVCCSA-L 0.000 description 1
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 1
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000011282 acid tar Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- DALDUXIBIKGWTK-UHFFFAOYSA-N benzene;toluene Chemical compound C1=CC=CC=C1.CC1=CC=CC=C1 DALDUXIBIKGWTK-UHFFFAOYSA-N 0.000 description 1
- 150000001555 benzenes Chemical class 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000020335 dealkylation Effects 0.000 description 1
- 238000006900 dealkylation reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 125000003454 indenyl group Chemical class C1(C=CC2=CC=CC=C12)* 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- QNGNSVIICDLXHT-UHFFFAOYSA-N para-ethylbenzaldehyde Natural products CCC1=CC=C(C=O)C=C1 QNGNSVIICDLXHT-UHFFFAOYSA-N 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001698 pyrogenic effect Effects 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A process for preparing benzene-series arylhydrocarbon from crude benzene includes such steps as proportionally adding common triplet oil, hydrorefining, fractionating, extracting in solvent, distilling and rectifying to obtain high-purity (more than 99.9%) benzene, toluene and xylene.
Description
One. technical field
The invention belongs to chemical field, relate to the deep processing and the utilization of the by product (crude benzol) of iron and steel enterprise and coking enterprise generation, particularly relating to a kind of is raw material with full cut crude benzol, obtains the method for aromatic hydrocarbons such as grade oil benzene,toluene,xylene.
Two. background technology
Benzene,toluene,xylene all is important organic chemical industry's basic raw material, and they mainly come from petroleum refining process.Crude benzol is to reclaim a kind of benzoline that obtains from the pyrogenic raw gas of coal, and main component is a mononuclear aromatics.Benzene,toluene,xylene content in the crude benzol accounts for more than 90%, wherein benzene account for 70%, toluene 8%～25%, dimethylbenzene 2%～5%.The benzene,toluene,xylene that obtains from crude benzol can be used for remedying the deficiency of benzene series produce market.
At present, the method by preparing benzene aromatic hydrocarbon by crude benzene mainly contains two kinds: a kind of is vitriol oil acid wash, and another kind is the shortening method.The acid wash technical process is simple, flexible operation, equipment are simple, material is easy to get.But can only partly remove sulfocompound and impurity in the crude benzol, aromatic hydroxy compound purity is not high in the course of processing, loss is bigger, and processing by-product acid tar and residue can cause serious environmental to pollute.This method is in the use that has been under an embargo of some developed countries.And the most of producer of China is still in this method of employing.
Since the 1950's, states such as American and Britain, moral, method succeed in developing crude benzol catalytic hydrofinishing method in succession.The sixties in 20th century, U.S. Hu Deli air products company succeeds in developing high temperature crude benzole hydrogenation process for refining (Litol method) system purified petroleum benzin, this technology at high temperature (600～630 ℃), high pressure (under 5.7～6.0MPa) by hydrofining and dealkylation, producing purity is 99.9%, the purified petroleum benzin product of S＜0.5ppm, the benzaldehyde product yield reaches 114%.But the Litol method need be operated under High Temperature High Pressure, and equipment and pipe material are required height, and investment is big, can only produce a kind of product, and economic benefit is relatively poor.To the eighties in 20th century, the U.S. and Germany succeed in developing low temperature hydrogenation purification techniques in the crude benzol (sulfolane process and KK method) again in succession, this technology at middle low temperature (320～380 ℃), middle pressure (under 3.5～3.7MPa) by hydrofining and extractive distillation, produce benzene, toluene and dimethylbenzene product, product purity 〉=99.9%, S＜0.5ppm, yield is about 98%.By the product purity height that the hydrofining method makes, S content is low, yield height, non-environmental-pollution.Two kinds of solvent method crude benzole hydrogenation process conditionss relax, invest low than the Litol method, better economic benefit.
Three kinds of crude benzole hydrogenation technologies all need independently to build a complete set of process system, because the technological process more complicated, plant capacity will reach that scale just can obtain favorable economic benefit more than 50,000 tons/year.And three kinds of crude benzole hydrogenation technologies all need the crude benzol raw material is carried out prefractionation, because crude benzol is extremely unstable, very easily polymerization when heating, coking are difficult to long-term operation.
Three. summary of the invention
The object of the present invention is to provide a kind of by in full cut crude benzol raw material, mixing atmosphere 3rd side cut oil, from full cut crude benzol, obtain the grade oil benzene,toluene,xylene through processes such as hydrofining, fractionation, solvent extraction distillation and rectifying, and the method for hydro-refining unit energy long-term operation.
The objective of the invention is to be achieved through the following technical solutions, a kind of method by preparing benzene aromatic hydrocarbon by crude benzene, it is characterized in that: full cut crude benzol raw material mixes atmosphere 3rd side cut oil after filtering, the weight ratio of crude benzol raw material and atmosphere 3rd side cut oil is 1: 9～9: 1, hydrogenation reaction takes place with hydrogen in the mixing raw material oil of crude benzol and atmosphere 3rd side cut oil in the hydrogenator of selective hydrogenation catalyst is housed, reaction conditions is: 300～360 ℃ of temperature, hydrogen pressure 2.0～3.5MPa, liquid air speed 1.0～2.0h
-1, hydrogen-oil ratio 500: 1～1000: 1; The effusive gas-liquid mixture of hydrogenator obtains hydrogenated oil behind gas-liquid separation, stripping; Hydrogenated oil is sent into separation column, and fractionator overhead is isolated the hydrogenated oil cut, isolates the atmosphere 3rd side cut oil distillate at the bottom of the fractionation Tata; The atmosphere 3rd side cut oil distillate is squeezed into the crude benzol feed(raw material)inlet again through pump, mixes to recycle with the crude benzol raw material; The hydrogenated oil cut enters weight-removing column, and the weight-removing column cat head is isolated the cut that contains benzene,toluene,xylene; The weight-removing column overhead fraction that contains benzene,toluene,xylene obtains grade oil aromatic hydrocarbons through fore-distillation, solvent extraction distillation and rectifying.
Contain Unstable Substances such as a small amount of diolefine, vinylbenzene, indenes, indane, colloid in the crude benzol, the heterocyclic nitrogen compound and the sulfide that also contain promotion diolefine and styrene polymerization, coking, crude benzol all easily produces black precipitate when normal temperature and heating, crude benzol advances before the hydrogenator, coking fast in interchanger and furnace tubing, running period is shorter.By in the crude benzol raw material, mixing a certain proportion of atmosphere 3rd side cut oil, make the mixing raw material of crude benzol and atmosphere 3rd side cut oil enter reactor with vapour, liquid mixed phase below 360 ℃, thereby delay the polymerization rate of Unstable Substances such as diolefine, the mobile part macromole Unstable Substance of taking away by liquid phase simultaneously, the hydrogenation unit one-time continuous can be extended to half a year running period more than.And the atmosphere 3rd side cut oil distillate can be recycled, and can not increase production cost.
The straight-run diesel oil that atmosphere 3rd side cut oil is produced for refinery's atmospheric and vacuum distillation unit, its flow process scope is about 210 ℃～365 ℃.
Selective hydrogenation catalyst can adopt molybdenum nickel tungsten phosphorus series catalysts, molybdenum nickel catalyst, molybdenum cobalt series catalyst, molybdenum cobalt phosphorus series catalysts etc., preferably select molybdenum cobalt phosphorus series catalysts for use, its effect is hydrogenation and removing sulphur, nitrogen impurity, the hydrogenation saturation of olefins, and the aromatic hydrocarbons saturation exponent is little.
The gas-liquid mixture of discharging from hydrogenator contains hydrogen sulfide, ammonia etc. through the liquid phase oil that gas-liquid separation obtains, they are that itself exists in the crude benzol raw material, or the organosulfur in the crude benzol raw material and organic amine produce in the shortening process, can remove by sophisticated steam stripping technique.
In the weight-removing column overhead fraction except benzene,toluene,xylene is arranged, also have many alkane such as normal hexane, normal heptane, 2.2-dimethylpropane, 2.4-dimethylpentane, 2.3.4-trimethylpentane etc., they are to exist in the crude benzol raw material or generate in catalytic hydrogenation reaction.These alkane can generate azeotrope with benzene, toluene or dimethylbenzene.Therefore, can not use common distillating method to tell benzene,toluene,xylene, must adopt solvent extraction distillatory method, obtain alkane (non-aromatics) and be dissolved with the solvent of aromatic hydrocarbons, non-aromatics is just separated with aromatic hydrocarbons.Extraction solvent can be selected N-Methyl pyrrolidone, diethylene glycol ether (glycol ether), triethylene glycol ether (triglycol), tetraethylene glycol (Tetraglycol 99), tetramethylene sulfone etc. for use; dimethyl sulfoxide (DMSO), N-formyl morpholine etc.; better select tetramethylene sulfone, N-N-formyl morpholine N-for use, preferably select the N-N-formyl morpholine N-for use.
The present invention need not the crude benzol raw material carried out treating processess such as prefractionation, the adaptability of raw material is strong, the device cycle of operation is long, can process the full cut crude benzol that reclaims in the raw gas from any one iron and steel enterprise or coking enterprise by-product when the coal tar, operational condition changes little, and the device one-time continuous can reach more than half a year running period.
Equipment used of the present invention can be made with extra care and the extracting rectifying device by newly-built complete crude benzole hydrogenation, also can utilize the existing installation of hydrogenation workshop, refinery and reforming plant.
The relative prior art of the present invention has following advantage:
1, the crude benzol raw material need not through prefractionation and pre-hydrogenation process, and whole crude benzole hydrogenation device required equipment reduces, and facility investment is low;
2, atmosphere 3rd side cut oil can directly be bought to the refinery, and can be recycled, and can not increase production cost.After having mixed a certain proportion of atmosphere 3rd side cut oil simultaneously, crude benzol mixing raw material hydrogenated oil cat head load in separation column reduces the separation column easy handling.
3, by in the crude benzol raw material, mixing a certain proportion of atmosphere 3rd side cut oil, the crude benzol mixing raw material exists with vapour, liquid mixed phase in interchanger, heating furnace tube and reactor and reacts, thereby delay the polymerization rate of Unstable Substances such as diolefine greatly, the mobile part macromole Unstable Substance of taking away by liquid phase simultaneously, the hydrogenation unit one-time continuous can be extended to half a year running period more than.
4, aromatic hydrocarbon product purity height, the purity of benzene, toluene, xylol all can reach more than 99.9%;
5, sulphur in the aromatic hydrocarbon product, nitrogen impurity content are low, all less than 1ppm.
Four. description of drawings
Fig. 1 is the schema that crude benzol is produced aromatic hydrocarbons;
Among the figure, the 1st, process furnace, the 2nd, reactor, the 3rd, gas-liquid separator, the 4th, stripping tower, the 5th, separation column, the 6th, weight-removing column, the 7th, pre-distillation column, the 8th, extraction distillation column, the 9th, stripping tower, the 10th, purified petroleum benzin tower, the 11st, benzenol hydrorefining.
Five. embodiment
The present invention is further illustrated below in conjunction with embodiment:
Embodiment 1:
Embodiment 2:
Embodiment 3:
Embodiment 4
Raw materials used with embodiment 1, its character sees Table 1.The character and the group composition of hydrogenation conditions, hydrogenated oil see Table 2.Other reaction conditionss, reactions steps are with embodiment 1.Product property sees Table 3.
The raw material that the present invention is simple relatively is a crude benzol, and under the reaction conditions same case, to comparing the running period of equipment therefor in the reaction, it is as follows to have done one group of contrast experiment:
Raw material is a crude benzol, and hydrogenation conditions, reactions steps are with embodiment 1.Test-results sees Table 4.
Raw material be crude benzol and atmosphere 3rd side cut oil by 1: 9 weight ratio mixing oil, hydrogenation conditions, reactions steps are with embodiment 1.Test-results sees Table 4.
Embodiment 6
Raw material is a crude benzol, and hydrogenation conditions, reactions steps are with embodiment 2.Test-results sees Table 4.
Raw material be crude benzol and atmosphere 3rd side cut oil by 2: 1 weight ratio mixing oils, hydrogenation conditions, reactions steps are with embodiment 2.Test-results sees Table 4.
Embodiment 7
Raw material is a crude benzol, and hydrogenation conditions, reactions steps are with embodiment 3.Test-results sees Table 4.
Raw material be crude benzol and atmosphere 3rd side cut oil by 9: 1 weight ratio mixing oils, hydrogenation conditions, reactions steps are with embodiment 3.Test-results sees Table 4.
Table 1, mixing raw material oil nature
Table 2, hydrogenated oil character and group composition
Table 3, aromatic hydrocarbon product character
| Project | Benzene | Toluene | Xylol |
| Outward appearance | Water-white is transparent | Water-white is transparent | Water-white is transparent |
| Purity, m% | ＞99.99 | ＞99.99 | ＞99.99 |
| Total sulfur, ppm | ＜1 | ＜1 | ＜1 |
| Total nitrogen, ppm | ＜1 | ＜1 | ＜1 |
Table 4, comparative test result
From embodiment 5,6,7 as can be seen, behind the adding atmosphere 3rd side cut oil, be increased to thousands of hour from tens hours the running period of device, increased more than tens times.
Claims (3)
1, a kind of method by preparing benzene aromatic hydrocarbon by crude benzene, it is characterized in that: full cut crude benzol raw material mixes atmosphere 3rd side cut oil after filtering, the crude benzol raw material is 1: 9～9: 1 with atmosphere 3rd side cut weight of oil ratio, hydrogenation reaction takes place with hydrogen in this mixing raw material oil in the hydrogenator of selective hydrogenation catalyst is housed, reaction conditions is: 300～360 ℃ of temperature, hydrogen pressure 2.0～3.5MPa, liquid air speed 1.0～2.0h
-1, hydrogen-oil ratio 500: 1～1000: 1; The effusive gas-liquid mixture of hydrogenator obtains hydrogenated oil behind gas-liquid separation, stripping; Hydrogenated oil is sent into separation column, and fractionator overhead is isolated the hydrogenated oil cut, isolates the atmosphere 3rd side cut oil distillate at the bottom of the fractionation Tata; The atmosphere 3rd side cut oil distillate is squeezed into the crude benzol feed(raw material)inlet again through pump, mixes to recycle with the crude benzol raw material; The hydrogenated oil cut enters weight-removing column, and the weight-removing column cat head is isolated the cut that contains benzene,toluene,xylene; The weight-removing column overhead fraction that contains benzene,toluene,xylene obtains grade oil aromatic hydrocarbons through fore-distillation, solvent extraction distillation and rectifying.
2, method according to claim 1 is characterized in that: described selective hydrogenation catalyst is molybdenum nickel tungsten phosphorus series catalysts, molybdenum nickel catalyst or molybdenum cobalt series catalyst or molybdenum cobalt phosphorus series catalysts.
3, method according to claim 1 is characterized in that: described selective hydrogenation catalyst is a molybdenum cobalt phosphorus series catalysts.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101368571A CN100445243C (en) | 2006-12-06 | 2006-12-06 | Method for producing benzene arenes from coarse benzene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101368571A CN100445243C (en) | 2006-12-06 | 2006-12-06 | Method for producing benzene arenes from coarse benzene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101028985A CN101028985A (en) | 2007-09-05 |
| CN100445243C true CN100445243C (en) | 2008-12-24 |
Family
ID=38714554
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006101368571A Active CN100445243C (en) | 2006-12-06 | 2006-12-06 | Method for producing benzene arenes from coarse benzene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100445243C (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101445420B (en) * | 2008-12-25 | 2012-02-22 | 上海奥韦通工程技术有限公司 | Process for preparing benzene aromatic hydrocarbon by crude benzene |
| CN102041030B (en) * | 2011-01-13 | 2013-07-03 | 中国石油天然气股份有限公司 | Method for controlling ultrahigh final boiling point of blending component of reformed high-octane gasoline |
| BR112013024420A2 (en) * | 2011-03-25 | 2016-12-20 | Chiyoda Corp | method for the production of single ring aromatic hydrocarbons |
| CN102703109A (en) * | 2012-05-30 | 2012-10-03 | 中国石油集团工程设计有限责任公司北京分公司 | Method for removing sulfur from crude oil by gas stripping method |
| CN103449955B (en) * | 2013-08-29 | 2015-05-20 | 邢台旭阳煤化工有限公司 | Method for extracting triphen from coker naphtha |
| CN103483138B (en) * | 2013-09-27 | 2015-11-18 | 山西焦化股份有限公司 | A kind of return preparation of crude benzene method and device |
| CN103910596B (en) * | 2013-12-04 | 2016-02-10 | 徐州龙辉化工科技有限公司 | Full cut crude benzene hydrogenation method and catalyzer |
| CN104725178A (en) * | 2015-02-04 | 2015-06-24 | 沾化瑜凯新材料科技有限公司 | Rectification process for preparing benzene, methylbenzene and dimethylbenzene from crude benzene |
| ITUB20152258A1 (en) * | 2015-07-17 | 2017-01-17 | Eurotecnica Melamine Luxemburg Zweigniederlassung In Ittigen | Process for the production of melamine with separation and recovery of high purity CO2 and NH3 |
| CN111154505B (en) * | 2018-11-08 | 2021-08-06 | 中国石油化工股份有限公司 | Coal tar hydrotreating process |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1587241A (en) * | 2004-07-26 | 2005-03-02 | 徐守忠 | Process for producing mixed benzene in removnig impurity in coarse benzene by catalytic purification |
-
2006
- 2006-12-06 CN CNB2006101368571A patent/CN100445243C/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1587241A (en) * | 2004-07-26 | 2005-03-02 | 徐守忠 | Process for producing mixed benzene in removnig impurity in coarse benzene by catalytic purification |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101028985A (en) | 2007-09-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100445243C (en) | Method for producing benzene arenes from coarse benzene | |
| CN100378046C (en) | Method for producing benzene aromatic hydrocarbon from crude benzole | |
| CN1900033A (en) | Method for producing benzene aromatic hydrocarbon from crude benzole | |
| CN101712889B (en) | Method for preparing light aromatics from coal tar | |
| CN101219918B (en) | Method for refining carbonization crude benzole | |
| CN101824336B (en) | Technique for producing terphenyl, indane and aromatics solvent oil by cracking C9 fraction and hydrogenation | |
| CN103361118B (en) | Method for recovering aromatic hydrocarbons from gasoline containing olefin and sulfide | |
| CN101445420B (en) | Process for preparing benzene aromatic hydrocarbon by crude benzene | |
| CN103305269B (en) | Method for producing gasoline and diesel by directly hydrogenating medium and low temperature coal tar | |
| CN113185996A (en) | Multi-stage cross flow extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid | |
| CN102382678B (en) | Method for producing aromatic hydrocarbon from coked gasoline | |
| CN107365241A (en) | A kind of crude benzole hydrogenation process for refining | |
| CN102336622B (en) | Reclaiming device and separation method for heavy component residue of coked crude benzene hydrogenation process | |
| CN113201364A (en) | Multi-stage countercurrent extraction device and method for catalyzing diesel polycyclic aromatic hydrocarbon by using ionic liquid | |
| CN101514136B (en) | Method for preparing high purity toluene from coking crude benzene | |
| CN104031679A (en) | Method for production of olefin and aromatic hydrocarbon from naphtha | |
| CN102001906A (en) | Coked crude benzene refining method | |
| CN204509216U (en) | Catalytically cracked gasoline extracting rectifying desulfurizer | |
| CN111748373B (en) | High-yield device and method for low-carbon olefins and aromatic hydrocarbons | |
| CN104355959A (en) | Production process for producing benzene aromatic hydrocarbons from coking crude benzene | |
| CN104672043A (en) | Light benzene hydrogenation method | |
| CN1064390C (en) | Double-solvant extraction for inferior paraffin base oil | |
| CN103789035A (en) | Method for heavy benzene hydrogenation to produce clean fuel oil | |
| CN1193969C (en) | Low temperature and low pressure hydrofining process for production of high quality n-hexane | |
| CN114085683A (en) | Process for preparing lubricating oil base oil by hydrogenating and regenerating waste lubricating oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20070905 Assignee: HUNAN ZHONGLING CHEMICAL Co.,Ltd. Assignor: HUNAN CHANGLING PETROCHEMICAL TECHNOLOGY DEVELOPMENT Co.,Ltd. Contract record no.: 2014430000033 Denomination of invention: Method for producing benzene aromatic hydrocarbon from crude benzole Granted publication date: 20081224 License type: Exclusive License Record date: 20140416 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 414012 Lu Kou Zhen Chang Lian Long Kou, Yunxi District, Yueyang City, Hunan Province (opposite to Chang Lian hospital) Patentee after: Hunan Changlian New Materials Technology Co.,Ltd. Country or region after: China Address before: 414012 intersection Town, Yunxi District, Hunan, Yueyang Patentee before: HUNAN CHANGLING PETROCHEMICAL TECHNOLOGY DEVELOPMENT Co.,Ltd. Country or region before: China |