CN108002974A - The process of refined coking crude benzene - Google Patents
The process of refined coking crude benzene Download PDFInfo
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- CN108002974A CN108002974A CN201711353821.3A CN201711353821A CN108002974A CN 108002974 A CN108002974 A CN 108002974A CN 201711353821 A CN201711353821 A CN 201711353821A CN 108002974 A CN108002974 A CN 108002974A
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 177
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000004939 coking Methods 0.000 title claims abstract description 22
- UAEPNZWRGJTJPN-UHFFFAOYSA-N methylcyclohexane Chemical compound CC1CCCCC1 UAEPNZWRGJTJPN-UHFFFAOYSA-N 0.000 claims abstract description 45
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 238000000895 extractive distillation Methods 0.000 claims abstract description 6
- 239000002904 solvent Substances 0.000 claims description 30
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 27
- 238000000605 extraction Methods 0.000 claims description 26
- 229910052739 hydrogen Inorganic materials 0.000 claims description 16
- 239000001257 hydrogen Substances 0.000 claims description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 10
- LCEDQNDDFOCWGG-UHFFFAOYSA-N N-Formyl-Morpholine Natural products O=CN1CCOCC1 LCEDQNDDFOCWGG-UHFFFAOYSA-N 0.000 claims description 3
- 125000003118 aryl group Chemical group 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- YNAVUWVOSKDBBP-UHFFFAOYSA-N Morpholine Chemical compound C1COCCN1 YNAVUWVOSKDBBP-UHFFFAOYSA-N 0.000 claims 2
- 238000004458 analytical method Methods 0.000 abstract description 14
- 239000000126 substance Substances 0.000 abstract description 3
- 239000005416 organic matter Substances 0.000 abstract description 2
- 238000004821 distillation Methods 0.000 description 18
- 238000003556 assay Methods 0.000 description 14
- 239000003381 stabilizer Substances 0.000 description 14
- 239000002994 raw material Substances 0.000 description 9
- 238000009834 vaporization Methods 0.000 description 9
- 230000008016 vaporization Effects 0.000 description 9
- 229910003460 diamond Inorganic materials 0.000 description 7
- 239000010432 diamond Substances 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 7
- 238000005070 sampling Methods 0.000 description 7
- 239000003208 petroleum Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- MMEYPSTUCSIDCF-UHFFFAOYSA-N benzene;methylcyclohexane Chemical compound C1=CC=CC=C1.CC1CCCCC1 MMEYPSTUCSIDCF-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000011265 semifinished product Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of process of refined coking crude benzene, belong to the purity analysis technical field of organic matter.The technological process that it includes is hydrogenation reaction, extractive distillation and rectifying, hydrogenation reaction is to be reacted in the secondary hydrogenation of pre-reactor and main reactor, product after reaction is cooled to liquid hydrogenated oil, the outlet temperature of pre-reactor is more than 202 DEG C, the outlet temperature of main reactor is more than 306 DEG C, mass percentage content≤0.7% of hexahydrotoluene in liquid hydrogenated oil.Outlet temperature of the invention by controlling reactor, to control hydrogenation reaction temperature, reduce the generation of accessory substance to the greatest extent, and the hexahydrotoluene content in hydrogenated oil and the regular indices for controlling extractant are controlled after the hydrogenation reaction, ensure hexahydrotoluene being sufficiently separated in benzene, hexahydrotoluene content is less than 150ppm in the petrobenzene being finally prepared.
Description
Technical field
The present invention relates to refining for coking crude benzene, belong to the purity analysis technical field of organic matter, more particularly to one kind
The process of refined coking crude benzene.
Background technology
Benzene and toluene and dimethylbenzene are all very important industrial chemicals, the stone being mainly derived from petrochemical process
Coking crude benzene in oily benzene and coking industry, above-mentioned coking crude benzene is by techniques such as purification ＆ isolations so as to obtain pure benzene and first
Benzene.At present.The process for refining of coking crude benzene mainly uses hydrofinishing method, and the hydrogenation technique of coking crude benzene, it includes pre- advanced
The de- weight of row, heavy benzol and light benzene are separated into by crude benzol, then are hydrogenated with light benzene, and light benzene carries out instead under the catalytic action of catalyst
Should, so that benzene, toluene and dimethylbenzene and other light hydrocarbon components are obtained, then by de- light processing, by above-mentioned mixture
Light components and reaction impurities removing, so as to obtain the mixtures such as the benzene of semi-finished product, toluene and non-aromatics, are also known as hydrogenated with
Oil, hydrogenated oil by extraction rectification technique, remove the non-aromatic component in hydrogenated oil, obtain the mixture of benzene and toluene, benzene again
It is passed through with the mixture of toluene in benzene knockout tower, you can separate benzene and toluene.
But hexahydrotoluene is easily produced in production technology is hydrogenated with, in the actual production process, to improve coking benzene
Quality, reduces hexahydrotoluene content in coking benzene, adjustment center of gravity is placed on extractive distillation unit and is adjusted, and is extracted by improving
Destilling tower temperature is taken, more non-aromaticss are steamed, but also causes a large amount of benzene to be brought into non-aromatics at the same time, in final coking benzene
Hexahydrotoluene content is generally in more than 180ppm, compared with petrobenzene (hexahydrotoluene content is less than 150ppm in petrobenzene)
Also certain gap.This method scope of application is narrow at the same time, when raw material components change, can not be adjusted to preferable at all
Value.
The content of the invention
In order to solve the above technical problems, the invention discloses a kind of refined Jiao for reducing hexahydrotoluene content in coking benzene
Change the process of crude benzol.
To achieve the above object, the invention discloses a kind of process of refined coking crude benzene, the technique stream that it includes
Journey is hydrogenation reaction, extractive distillation and rectifying, and the hydrogenation reaction is mixed into after including the heat exchange vaporization of crude benzol raw material with hydrogen
The hydrogenation reaction in hydrogenation reaction and main reactor is carried out in pre-reactor, the product after reaction adds through being cooled into liquid step by step
Hydrogen oil enters in stabilizer, it is characterised in that：The outlet temperature of the pre-reactor is more than 202 DEG C, the main reactor
Outlet temperature is more than 306 DEG C, and is sampled analysis to the liquid hydrogenated oil in the stabilizer, if the matter of hexahydrotoluene
Measure degree and be higher than 0.7%, then need to reduce the temperature of pre-reactor and main reactor, while temperature is reduced, pair add
Hydrogen in the gas-circulating system of hydrogen reaction is sampled analysis, controls hydrogen volume degree >=90%, until liquid
Hexahydrotoluene mass percentage content≤0.7% in state hydrogenated oil.
Further, liquid hydrogenated oil is separated into containing benzene, toluene and non-aromatics by pre-distillation column in the stabilizer
BT cuts and the XS cuts containing dimethylbenzene, the BT cuts are entered in extraction distillation column, extractant effect under, realize benzene with it is non-
The separation of aromatic hydrocarbons, volume percent content >=95% of the N- N-formyl morpholine Ns in the extractant.
Yet further, temperature is 120 DEG C when controlling extractant feed.
Further, if non-aromatics mass percentage content ＜ 3.5% in BT cuts, control solvent is than ＜ 7.0；
If non-aromatics mass percentage content≤4.5% in 3.5%≤BT cuts, 7.0≤solvent ratio≤7.5 are controlled；If BT cuts
In non-aromatics mass percentage content ＞ 4.5%, control 7.5 ＜ solvents ratio≤8.0, the solvent ratio for extractant with being extracted
Take the mass ratio of hydrogenated oil.
Further, the outlet temperature of the pre-reactor is 205 DEG C, and the outlet temperature of the main reactor is 310
℃。
As the preferred of technical solution of the present invention：
The outlet temperature of the pre-reactor is 205 DEG C, and the outlet temperature of the main reactor is 310 DEG C；
The extractant feed temperature control is 120 DEG C；It is 7.5 to control solvent ratio.
The present invention concrete technology flow process be：
Crude benzol mixes after entering preevaporator heat exchange vaporization with hydrogen, initially enters pre-reactor, then into main anti-
Device is answered to carry out secondary hydrogenation reaction, the product after hydrogenation reaction enters stabilizer, control stabilization by being cooled into liquid step by step
Hexahydrotoluene content (mass percent)≤0.7% in tower, if its content is higher than 0.7%, needs to reduce pre-reactor
With the temperature of main reactor, and outlet temperature is controlled by reducing reactor inlet temperature, wherein, reactor inlet temperature is every
1 DEG C is reduced, it is necessary to analysis is sampled to the hexahydrotoluene content in stabilizer, until content meets standard, in adjustment temperature
, it is necessary to be sampled analysis to recyclegas while spending, hydrogen content (percent by volume) must reach 90% in circulating air
More than, because amounts of hydrogen deficiency is easy to cause side reaction.
Hydrogenated oil in stabilizer is separated into containing benzene, toluene, BT cuts of non-aromatics and containing dimethylbenzene by pre-distillation column
XS cuts, wherein in non-aromatics be mainly hexahydrotoluene, BT cuts enter extraction distillation column, under the action of extractant,
Hexahydrotoluene and other non-aromaticss are produced from extractive distillation tower top, it is achieved thereby that the separation of benzene and hexahydrotoluene；
However, the effect of extracting of extractive distillation part is bad non-aromatics can be caused to separate, hexahydrotoluene can be by band
Into benzene, therefore, it is necessary to periodically chemically examine the N- N-formyl morpholine Ns in extractant, its state is fully grasped, it is e.g., its acid-base property, miscellaneous
Matter content etc., it is desirable to which extractant purity must not be less than 95%；Secondly, extractant temperature is adjusted, temperature height directly affects extraction
Efficiency is taken, to be adjusted according to sample result is done, then general temperature control adjusts solvent ratio at 120 DEG C or so, excessive
Solvent ratio can cause non-aromatics fully to volatilize, and too small solvent can cause the aromatic hydrocarbons such as benzene to be brought into non-aromatics than then, shadow
Ring the yield of benzene.Solvent ratio (extractant and the mass ratio being extracted between hydrogenated oil) generally 7.5 or so, specifically will according into
Material change of component is adjusted, if the non-aromatics mass percentage content ＜ 3.5% in BT cuts, control solvent is than ＜ 7.0；
If non-aromatics mass percentage content≤4.5% in 3.5%≤BT cuts, 7.0≤solvent ratio≤7.5 are controlled；If BT cuts
In non-aromatics mass percentage content ＞ 4.5%, control 7.5 ＜ solvents ratio≤8.0, it is non-aromatic in BT cuts in actual production
Hydrocarbon content is generally 4.5% or so, therefore solvent ratio is normally controlled in 7.5, and by stablizing extraction efficiency, hexahydrotoluene is smooth
Ground is deviate from from BT cuts, and hexahydrotoluene content is less than 150ppm in the coking benzene obtained by rectifying.
Beneficial effect：
Outlet temperature of the invention by controlling reactor, to control hydrogenation reaction temperature, reduces the production of accessory substance to the greatest extent
It is raw, and the hexahydrotoluene content in hydrogenated oil and the regular indices for controlling extractant are controlled after the hydrogenation reaction, ensure
Hexahydrotoluene being sufficiently separated in benzene, hexahydrotoluene content is less than 150ppm in the petrobenzene being finally prepared, should
Petrobenzene not only meets high-end chemical industry production needs, and it is per ton on sales price improve 150 yuan, add wound
Receive.
Embodiment
In order to preferably explain the present invention, below in conjunction with the specific embodiment main contents that the present invention is furture elucidated, but
Present disclosure is not limited solely to following embodiments.
Embodiment 1
After crude benzol raw material enters preevaporator heat exchange vaporization, reacted into pre-reactor, inlet temperature is 200 DEG C, outlet
Temperature is 205 DEG C, then becomes owner of reactor reaction by the way that diamond heating is laggard, inlet temperature is 275 DEG C, and outlet temperature is
306 DEG C, hydrogen content is 93% (volume percent content) in assay recyclegas, and at stabilizer bottom, sampling analysis is hydrogenated with
Hexahydrotoluene content is 0.65% (mass percentage content) in oil.
Hydrogenated oil is separated into BT cuts and XS cuts by pre-distillation column, and BT cuts enter extraction distillation column, assay
Non-aromatic hydrocarbon content is 4.5% (mass percentage content), and extractant and the mass ratio being extracted between hydrogenated oil are 7.5, solvent
Feeding temperature control is 120 DEG C, and hexahydrotoluene content is down to 95ppm in pure BT cuts after extraction, and pure BT cuts enter purified petroleum benzin
It is 140ppm that tower obtains hexahydrotoluene content in purified petroleum benzin by rectifying, reaches petrobenzene quality index.
Embodiment 2
After crude benzol raw material enters preevaporator heat exchange vaporization, reacted into pre-reactor, inlet temperature is 198 DEG C, outlet
Temperature is 202 DEG C, then becomes owner of reactor reaction by the way that diamond heating is laggard, inlet temperature is 275 DEG C, and outlet temperature is
306 DEG C, hydrogen content is 95% (volume percent content) in assay recyclegas, and at stabilizer bottom, sampling analysis is hydrogenated with
Hexahydrotoluene content is 0.60% (mass percentage content) in oil.
Hydrogenated oil is separated into BT cuts and XS cuts by pre-distillation column, and BT cuts enter extraction distillation column, assay
Non-aromatic hydrocarbon content is 4.0% (mass percentage content), and extraction tower solvent is 7.5 than control, and solvent feed temperature control is 120
DEG C, hexahydrotoluene content is down to 90ppm in pure BT cuts after extraction, and pure BT cuts obtain purified petroleum benzin into pure benzene tower by rectifying
Middle hexahydrotoluene content is 140ppm, reaches petrobenzene quality index.
Embodiment 3
After crude benzol raw material enters preevaporator heat exchange vaporization, reacted into pre-reactor, inlet temperature is 200 DEG C, outlet
Temperature is 205 DEG C, then becomes owner of reactor reaction by the way that diamond heating is laggard, inlet temperature is 280 DEG C, and outlet temperature is
310 DEG C, hydrogen content is 93% (volume percent content) in assay recyclegas, and at stabilizer bottom, sampling analysis is hydrogenated with
Hexahydrotoluene content is 0.60% (mass percentage content) in oil.
Hydrogenated oil is separated into BT cuts and XS cuts by pre-distillation column, and BT cuts enter extraction distillation column, assay
Non-aromatic hydrocarbon content is 3.2% (mass percentage content), and extraction tower solvent is 6.8 than control, and solvent feed temperature control is 120
DEG C, hexahydrotoluene content is down to 80ppm in pure BT cuts after extraction, and pure BT cuts obtain purified petroleum benzin into pure benzene tower by rectifying
Middle hexahydrotoluene content is 130ppm, reaches petrobenzene quality index.
Embodiment 4
After crude benzol raw material enters preevaporator heat exchange vaporization, reacted into pre-reactor, inlet temperature is 206 DEG C, outlet
Temperature is 215 DEG C, then becomes owner of reactor reaction by the way that diamond heating is laggard, inlet temperature is 290 DEG C, and outlet temperature is
318 DEG C, hydrogen content is 93% (volume percent content) in assay recyclegas, and at stabilizer bottom, sampling analysis is hydrogenated with
Hexahydrotoluene content is 0.75% (mass percentage content) in oil, then needs adjustment to reduce pre-reactor and main reactor
Temperature, and outlet temperature is controlled by reducing reactor inlet temperature, wherein, reactor inlet temperature often reduce by 1 DEG C, it is necessary to
Analysis is sampled to the hexahydrotoluene content in stabilizer, until content meets standard, finally, adjust pre-reactor into
Mouth temperature is 200 DEG C, and outlet temperature is 209 DEG C, and the inlet temperature of main reactor is 284 DEG C, and outlet temperature is 312 DEG C, is hydrogenated with
Hexahydrotoluene content is 0.69% in oil.
Hydrogenated oil is separated into BT cuts and XS cuts by pre-distillation column, and BT cuts enter extraction distillation column, assay
Non-aromatic hydrocarbon content is 4.6% (mass percentage content), and extraction tower solvent is 7.8 than control, and solvent feed temperature control is 120
DEG C, hexahydrotoluene content is down to 105ppm in pure BT cuts after extraction, and pure BT cuts are obtained pure into pure benzene tower by rectifying
Hexahydrotoluene content is 148ppm in benzene, reaches petrobenzene quality index.
Embodiment 5
After crude benzol raw material enters preevaporator heat exchange vaporization, reacted into pre-reactor, inlet temperature is 202 DEG C, outlet
Temperature is 210 DEG C, then becomes owner of reactor reaction by the way that diamond heating is laggard, inlet temperature is 280 DEG C, and outlet temperature is
310 DEG C, hydrogen content is 93% (volume percent content) in assay recyclegas, and at stabilizer bottom, sampling analysis is hydrogenated with
Hexahydrotoluene content is 0.70% (mass percentage content) in oil.
Hydrogenated oil is separated into BT cuts and XS cuts by pre-distillation column, and BT cuts enter extraction distillation column, assay
Non-aromatic hydrocarbon content is 4.5% (mass percentage content), and extraction tower solvent is 7.5 than control, and solvent feed temperature control is 120
DEG C, hexahydrotoluene content is down to 103ppm in pure BT cuts after extraction, and pure BT cuts are obtained pure into pure benzene tower by rectifying
Hexahydrotoluene content is 145ppm in benzene, reaches petrobenzene quality index.
Embodiment 6
After crude benzol raw material enters preevaporator heat exchange vaporization, reacted into pre-reactor, inlet temperature is 200 DEG C, outlet
Temperature is 205 DEG C, then becomes owner of reactor reaction by the way that diamond heating is laggard, inlet temperature is 280 DEG C, and outlet temperature is
310 DEG C, hydrogen content is 93% (volume percent content) in assay recyclegas, and at stabilizer bottom, sampling analysis is hydrogenated with
Hexahydrotoluene content is 0.67% (mass percentage content) in oil.
Hydrogenated oil is separated into BT cuts and XS cuts by pre-distillation column, and BT cuts enter extraction distillation column, assay
Non-aromatic hydrocarbon content is 4.6% (mass percentage content), and extraction tower solvent is 7.5 than control, and solvent feed temperature control is 120
DEG C, hexahydrotoluene content is down to 98ppm in pure BT cuts after extraction, and pure BT cuts obtain purified petroleum benzin into pure benzene tower by rectifying
Middle hexahydrotoluene content is 145ppm, reaches petrobenzene quality index.
Embodiment 7
After crude benzol raw material enters preevaporator heat exchange vaporization, reacted into pre-reactor, inlet temperature is 200 DEG C, outlet
Temperature is 205 DEG C, then becomes owner of reactor reaction by the way that diamond heating is laggard, inlet temperature is 280 DEG C, and outlet temperature is
310 DEG C, hydrogen content is 93% (volume percent content) in assay recyclegas, and at stabilizer bottom, sampling analysis is hydrogenated with
Hexahydrotoluene content is 0.62% (mass percentage content) in oil.
Hydrogenated oil is separated into BT cuts and XS cuts by pre-distillation column, and BT cuts enter extraction distillation column, assay
Non-aromatic hydrocarbon content is 3.6% (mass percentage content), and extraction tower solvent is 7.2 than control, and solvent feed temperature control is 120
DEG C, hexahydrotoluene content is down to 75ppm in pure BT cuts after extraction, and pure BT cuts obtain purified petroleum benzin into pure benzene tower by rectifying
Middle hexahydrotoluene content is 125ppm, reaches petrobenzene quality index.
Above example is only optimal citing, and is not the restriction to embodiments of the present invention.Except above-described embodiment
Outside, the present invention also has other embodiment.All technical solutions formed using equivalent substitution or equivalent transformation, all fall within the present invention
It is required that protection domain.
Claims (6)
1. a kind of process of refined coking crude benzene, the technological process that it includes is hydrogenation reaction, extractive distillation and rectifying, institute
It is to be reacted in the secondary hydrogenation of pre-reactor and main reactor to state hydrogenation reaction, and the product after reaction is cooled to liquid hydrogenated oil,
It is characterized in that：The outlet temperature of the pre-reactor is more than 202 DEG C, the outlet temperature of the main reactor for 306 DEG C with
On, mass percentage content≤0.7% of hexahydrotoluene in the liquid hydrogenated oil.
2. the process of coking crude benzene is refined according to claim 1, it is characterised in that：The liquid hydrogenated oil passes through pre-
Destilling tower is separated into the BT cuts containing benzene, toluene and non-aromatics and the XS cuts containing dimethylbenzene, and the BT cuts enter extraction and steam
Evaporate in tower, under extractant effect, realize the separation of benzene and non-aromatics, the extractant is N- N-formyl morpholine Ns, the N- formyls
Purity >=95% of morpholine.
3. the process of coking crude benzene is refined according to claim 2, it is characterised in that：The extractant feed temperature is controlled to be
120℃。
4. the process of coking crude benzene is refined according to claim 2, it is characterised in that：If the non-aromatic hydrocarbonaceous in BT cuts
Degree ＜ 3.5% is measured, then solvent is than ＜ 7.0；Non-aromatics mass percentage content in 3.5%≤BT cuts≤
4.5%, 7.0≤solvent ratio≤7.5；Non-aromatics mass percentage content ＞ 4.5% in BT cuts, 7.5 ＜ solvents ratios≤
8.0, the solvent is than for extractant and the mass ratio for being extracted hydrogenated oil.
5. according to the process of the 1 or 2 or 3 or 4 refined coking crude benzene of claim, it is characterised in that：The pre-reaction
The outlet temperature of device is 205 DEG C, and the outlet temperature of the main reactor is 310 DEG C.
6. according to the process of the 1 or 2 or 3 or 4 refined coking crude benzene of claim, it is characterised in that：Hydrogenation reaction
Hydrogen volume degree >=90% in gas-circulating system.
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2017
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