CN1329487C - Hydrogen free isomerization upgrading process for low bracker gasoline - Google Patents
Hydrogen free isomerization upgrading process for low bracker gasoline Download PDFInfo
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- CN1329487C CN1329487C CNB2003101058340A CN200310105834A CN1329487C CN 1329487 C CN1329487 C CN 1329487C CN B2003101058340 A CNB2003101058340 A CN B2003101058340A CN 200310105834 A CN200310105834 A CN 200310105834A CN 1329487 C CN1329487 C CN 1329487C
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- 238000000034 method Methods 0.000 title claims abstract description 44
- 230000008569 process Effects 0.000 title claims abstract description 39
- 239000001257 hydrogen Substances 0.000 title claims description 25
- 229910052739 hydrogen Inorganic materials 0.000 title claims description 25
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims description 20
- 238000006317 isomerization reaction Methods 0.000 title abstract description 8
- 239000000047 product Substances 0.000 claims abstract description 46
- 238000010521 absorption reaction Methods 0.000 claims abstract description 44
- 239000003381 stabilizer Substances 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 19
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 19
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 3
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 36
- 239000007789 gas Substances 0.000 claims description 31
- 238000006243 chemical reaction Methods 0.000 claims description 23
- 238000003795 desorption Methods 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000009834 vaporization Methods 0.000 claims description 9
- 230000008016 vaporization Effects 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 7
- 239000002283 diesel fuel Substances 0.000 claims description 7
- 230000002745 absorbent Effects 0.000 claims description 6
- 239000002250 absorbent Substances 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 230000003197 catalytic effect Effects 0.000 claims description 5
- 239000002808 molecular sieve Substances 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 2
- 238000007634 remodeling Methods 0.000 claims description 2
- 230000004048 modification Effects 0.000 abstract description 7
- 238000012986 modification Methods 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 230000002349 favourable effect Effects 0.000 abstract 1
- 238000010992 reflux Methods 0.000 abstract 1
- 238000005520 cutting process Methods 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 238000012545 processing Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010079 rubber tapping Methods 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention mainly relates to an isomerization modification technique for low bracket gasoline, particularly to a non-hydrogenating isomerization modification technique for low bracket gasoline. The non-hydrogenating isomerization modification technique for low bracket gasoline comprises the following step: straight gasoline is delivered to a heating furnace by a pump and is fed in a reactor. The non-hydrogenating isomerization modification technique is mainly characterized in that underflow products of the reactor are delivered to a reboiler at the bottom of a stabilizer tower for heat interchange and then are fed in a heat exchanger for heat interchange, fed in a cooler for reaction products and fed in a gas-liquid separation pot for gas-liquid separation; the crude gasoline of the underflow products of the separation pot are pumped out by the pump to be fed to the upper part of an absorption tower, and gas-rich top flow products of the separation pot are fed to the lower part of the absorption tower whose top flow products are changed into gas to be exhausted and underflow products are pumped out by a pump at the bottom of the tower to be fed to the heat exchanger and then be fed in the middle of the stabilizer tower; top products of the stabilizer tower are cooled by the cooler and then are fed in a reflux pot, and liquid hydrocarbon as underflow products of the stabilizer tower is pumped out by a pump to be fed in the upper part of the stabilizer tower and/or fed in a collection pot of liquid hydrocarbon; isomerization modification gasoline as bottom products of the stabilizer tower is fed in the heat exchanger, then is fed in the heat exchanger and the cooler to be cooled and is fed in the top of the absorption tower and/or fed in a collection pot of isomerization modification gasoline. The present invention has the advantages of simple technique process, easy operation, small occupation area, little investment and favorable benefits.
Description
Technical field:
The present invention relates generally to low octane value gasoline isomery modifying process, relates in particular to low octane value gasoline non-hydrogen isomery modifying process.
Background technology:
Along with environmental requirement and national policy guiding, on the market stop bracket gasoline demand is constantly increased.China's regulation stops to produce doped fuel from January 1 calendar year 2001.On July 1st, 2000 stopped using and sold doped fuel, and will eliminate doped fuel in the short period of time, realize changing to clean fuel from polluting.The prior art boosting of octane rating mainly contains following several technology: 1. catalytic reforming process: this technological advantage is that gasoline octane rating can reach requirement, and shortcoming is that working condition harshness, product aromaticity content exceed standard, the investment cost height.2. face the full fraction isomeric upgrading of hydrogen (TIP) technology (Shell Oil Co.'s patent), the octane value of straight-run spirit can be brought up to more than the RON88 by the precious metal molecular sieve catalyst, owing to need hydrogen, investment cost height, corollary system complexity are used more abroad.3. adopting zeolite molecular sieve fractionation by adsorption and isomery upgrading to combine to produce the higher isoparaffin of octane value to mix converts in the gasoline.More than three kinds of technology ubiquity processing condition harshnesses, complicated operation, corollary system complexity, therefore investment is high, payback period is long.
The patent No. 92106253.2, name is called the patent of " non-hydro isomerizaiton process ", a kind of non-hydro isomerizaiton process is disclosed, this processing requirement stock oil straight-run spirit and contain cured diesel oil by 1: 1 mixed, temperature of reaction will need improve constantly temperature of reaction with the continuous reduction of catalyst activity, could keep reaction depth.Bring certain degree of difficulty to actual production.
Summary of the invention:
The objective of the invention is to avoid the deficiencies in the prior art part and a kind of low octane value gasoline non-hydrogen isomery modifying process is provided.This technology mainly adopts fixed bed adiabatic reactor, entire reaction course is under conditions of non-hydrogen, under the molecular sieve catalyst effect of modification, series of chemical such as petrol molecule optionally produces cracking, hydrogen transference, isomerization, cyclisation, aromizing, coincide, in reaction process, be high-octane component, gasoline octane rating is improved low-octane alkane upgrading.The comprehensive heat effect of above-mentioned reaction is an endothermic process.
Purpose of the present invention can be by realizing by the following technical solutions: a kind of low octane value gasoline non-hydrogen isomery modifying process, include straight-run spirit and be transported to process furnace (F-1) through pump (P-1), enter reactor (R-1), its principal feature is to send into interchanger (E-1) heat exchange again after the underflow product of reactor (R-1) is transported to stabilizer tower (T-2) end reboiler (E-7) heat exchange, dereaction product water cooler (E-2) enters catch pot (V-1) and carries out gas-liquid separation then; Separating tank (V-1) underflow product raw gasline is extracted out through pump (P-2) and is delivered to top, absorption tower (T-1), and its top apoblema rich gas goes to bottom, absorption tower (T-1); The top apoblema dry gas on absorption tower (T-1) is discharged; Absorption tower (T-1) underflow product enters stabilizer tower (T-2) middle part after interchanger (E-5) is delivered in column bottoms pump (P-3) extraction, its overhead product enters return tank (V-2) after water cooler (E-6) cooling, its underflow product liquid hydrocarbon is extracted out through pump (P-4), enters stabilizer tower (T-2) top and/or enters the liquid hydrocarbon holding tank; Stabilizer tower (T-2) bottom product isomery reformulated gasoline enters interchanger (E-5), then enters interchanger (E-3), water cooler (E-4) cooling, enters absorption tower (T-1) and pushes up and/or enter isomery reformulated gasoline holding tank.
The present invention also includes the reaction product after reboiler (E-7) heat exchange, and sends into interchanger (E-1) heat exchange after desorption tower (T-3) end reboiler (E-8) heat exchange again; After separating tank (V-1) top apoblema rich gas goes rich gas compressor (C-1) compression, with mix from the stripping gas on desorption tower (T-3) top and/or through the release underflow product rich absorbent oil of self-absorption tower (T-1) of pump (P-3), enter equilibrium vaporization jar (V-3) gas-liquid separation, jar (V-3) top apoblema compression rich gas enters bottom, absorption tower (T-1); Stingy self-absorption tower (T-1) top enters two-level absorption tower (T-4) bottom, and the absorption agent catalytic diesel oil enters top of tower, absorbs diesel oil behind the liquid hydrocarbon and goes out device at the bottom of by tower; Dry gas is discharged from two-level absorption tower (T-4) top; The condensate oil of equilibrium vaporization jar (V-3) is extracted out through fresh feed pump (P-5) and is delivered to interchanger (E-3) heat exchange, enters desorption tower (T-3) top then, and stripping gas advances equilibrium vaporization jar (V-3) from desorption tower (T-3) top; The rich absorbent oil at desorption tower (T-3) end enters stabilizer tower (T-2) middle part after fresh feed pump (P-6) is delivered to interchanger (E-5) heat exchange.
The underflow product that described low octane value gasoline non-hydrogen isomery modifying process further comprises the device that responds (R-1) can be transported to process furnace (F-2), enters reactor (R-2), and its underflow product is transported to stabilizer tower (T-2) end reboiler (E-7) heat exchange.
The reaction pressure of described low octane value gasoline non-hydrogen isomery modifying process is 0.1-1.05Mpa; Temperature of reaction is 300-440 ℃; Reaction velocity is 0.2-0.8 (V) hr
-1
The present invention has catalyzer in reactor (R-1), (R-2), catalyzer is the molecular sieve catalyst ZSM-5 of remodeling.
Reactor of the present invention is a fixed bed adiabatic reactor.
Described low octane value gasoline non-hydrogen isomery modifying process absorption tower (T-1) pressure is 0.08-1.3MPa, and temperature is 30-60 ℃; Stabilizer tower (T-2) reaction pressure is 0.8-1.3MPa, and temperature is 50-180 ℃; Desorption tower (T-3) pressure is 0.8-1.3MPa, and temperature is 60-130 ℃; Two-level absorption tower (T-4) pressure is 0.7-1.3MPa, and temperature is 30-50 ℃.
Described feed gasoline includes the recovery lighter hydrocarbons of straight-run spirit, coker gasoline, pressure gasoline, oil-gas field.
The invention has the beneficial effects as follows,
This technology can increase substantially the octane value of low octane value gasoline, the octane value of straight-run spirit is about RON50-65 before processing, the octane value (RON) of handling the back reformulated gasoline increases by 20～30 units, reaches 84～88, adds a small amount of octane promoter and just can reach 90 (#) gasoline.Strong to adaptability to raw material, catalyzer one way long reaction time, coking is few, regeneration times is few, entire life is long; Non-hydrogen fixed bed reaction, operational condition relax, the simple operation easily of technical process; Floor space is little, less investment, profitable.
Description of drawings:
Fig. 1 is the embodiment of the invention 1 a low octane value gasoline non-hydrogen isomery modifying process schema (double tower);
Fig. 2 is the embodiment of the invention 2 low octane value gasoline non-hydrogen isomery modifying process schemas (four towers).
Among the figure: E is an interchanger; F is a process furnace; R is a reactor; V is a container; T is a tower; P is a pump; C is a compressor.
Embodiment:
Be described in further detail below in conjunction with the most preferred embodiment shown in the accompanying drawing:
Embodiment 1: see Fig. 1, and low octane value gasoline non-hydrogen isomery modifying process (double tower), low octane value gasoline is transported to process furnace F-1 through pump P-1, enters reactor R-1.Under catalyst action, low octane value gasoline carries out the reaction of isomery upgrading.Because reaction is for thermo-negative reaction,, finishes the isomery upgrading and react so oil gas enters reactor R-2 again through process furnace F-2 heating after one section reaction.Its underflow product is transported to reboiler E-7 heat exchange at the bottom of the stabilizer tower T-2.Send into interchanger E-1 heat exchange at the bottom of the stabilizer tower T-2 after the reboiler E-7 heat exchange again, dereaction product water cooler E-2 enters catch pot V-1 and carries out gas-liquid separation then.Separating tank V-1 underflow product raw gasline is extracted out through pump P-2 and is delivered to T-1 top, absorption tower, and its top apoblema rich gas goes to T-1 bottom, absorption tower.Absorption agent absorbs liquid hydrocarbon contained in the gas get off.The top apoblema dry gas of absorption tower T-1 is discharged; Absorption tower T-1 underflow product enters stabilizer tower T-2 middle part after interchanger E-5 is delivered in column bottoms pump P-3 extraction, its overhead product enters return tank V-2 after water cooler E-6 cooling.Its underflow product liquid hydrocarbon is extracted out through pump P-4, enters stabilizer tower T-2 top and/or enters the liquid hydrocarbon holding tank; Stabilizer tower T-2 bottom product isomery reformulated gasoline enters interchanger E-5, then enters interchanger E-3, water cooler E-4 cooling, enters absorption tower T-1 top and/or enters isomery reformulated gasoline holding tank.
Its processing condition see Table 1, table 2, table 3.
Process furnace table 1
| Sequence number | Project | F-1 | F-2 |
| 1 | Advance furnace pressure power Mpa (cutting off) | 0.8-1.45 | 0.47-1.0 |
| 2 | Pressure Mpa (cutting off) comes out of the stove | 0.5-1.05 | 0.3-0.67 |
| 3 | Advance furnace temperature ℃ | 180-221 | 270-410 |
| 4 | Tapping temperature ℃ | 300-440 | 300-440 |
Reactor table 2
| Sequence number | Project | R-1 | R-2 |
| 1 | Temperature ℃ | ||
| The initial stage～phase not | 300～440 | 300～440 | |
| 2 | Bed temperature drop ℃ | 20～30 | 10～30 |
| 3 | Pressure Mpa (cutting off) | ||
| The top | 0.5 | 0.3 | |
| Regeneration | 0.2 | 0.15 | |
| 4 | Bed pressure drop Mpa (cutting off) | 0.03 | 0.03 |
| 5 | Air speed (V) hr- 1 | 0.2-0.8 | 0.2-0.8 |
3, tower table 3
| Sequence number | Project | T-1 | T-2 |
| 1 | Pressure MPa (cutting off) | ||
| Cat head | 0.08 | 0.8-1.3 | |
| At the bottom of the tower | 0.13 | 0.84-1.35 | |
| 2 | Temperature ℃ | ||
| Cat head | 30 | 50-60 | |
| At the bottom of the tower | 60 | 160-180 |
Embodiment 2: see Fig. 2, and low octane value gasoline non-hydrogen isomery modifying process (four towers), low octane value gasoline is transported to process furnace F-1 through pump P-1, enters reactor R-1.Under catalyst action, low octane value gasoline carries out the reaction of isomery upgrading.Because reaction is for thermo-negative reaction, so oil gas is again through two sections heating after one section reaction, the underflow product of reactor R-1 is transported to process furnace F-2, enters reactor R-2, finishes the isomery upgrading and reacts.Its underflow product is transported to reboiler E-7 heat exchange at the bottom of the stabilizer tower T-2.Underflow product after the reboiler E-7 heat exchange at the bottom of the stabilizer tower T-2 is sent into interchanger E-1 heat exchange earlier with after the reboiler E-8 heat exchange at the bottom of the desorption tower T-3 again; After separating tank V-1 top apoblema rich gas goes rich gas compressor C-1 compression, with mix from the stripping gas on desorption tower T-3 top and/or through the release underflow product rich absorbent oil of self-absorption tower T-1 of pump P-3, enter equilibrium vaporization jar V-3 gas-liquid separation, a jar V-3 top apoblema compression rich gas enters absorption tower T-1 bottom.Rich gas from bottom to top fully contacts on tower tray with top-down absorption agent, and absorption agent absorbs liquid hydrocarbon contained in the rich gas get off.Stingy self-absorption tower T-1 top enters two-level absorption tower T-4 bottom, and the absorption agent catalytic diesel oil enters top of tower, absorbs diesel oil behind the liquid hydrocarbon and goes out device at the bottom of by tower; Dry gas is discharged from two-level absorption tower T-4 top; The condensate oil of equilibrium vaporization jar V-3 is extracted out through fresh feed pump P-5 and is delivered to interchanger E-3 heat exchange, enters desorption tower T-3 top then, and stripping gas advances equilibrium vaporization jar V-3 from desorption tower T-3 top.Rich absorbent oil at the bottom of the desorption tower T-3 is delivered to feed exchanger E-5 heat exchange through fresh feed pump P-6 and is entered stabilizer tower T-2 middle part.In stabilizer tower, liquid hydrocarbon is separated with the isomery reformulated gasoline.Stabilizer tower ejects liquid hydrocarbon, goes out stable gasoline (being the isomery reformulated gasoline) at the bottom of the stabilizer tower.Its overhead product enters return tank V-2 after water cooler E-6 cooling, its product liquid hydrocarbon is extracted out through pump P-4, enters stabilizer tower T-2 top and/or enters the liquid hydrocarbon holding tank.Stabilizer tower T-2 bottom product isomery reformulated gasoline enters interchanger E-5, then enters interchanger E-3, water cooler E-4 cooling, enters absorption tower T-1 top and/or enters isomery reformulated gasoline holding tank.
Its processing condition see Table 4, table 5, table 6.
Process furnace table 4
| Sequence number | Project | F-1 | F-2 |
| 1 | Advance furnace pressure power Mpa (cutting off) | 0.8-1.45 | 0.47-1.0 |
| 2 | Pressure Mpa (cutting off) comes out of the stove | 0.5-1.05 | 0.3-0.67 |
| 3 | Advance furnace temperature ℃ | 180-221 | 270-410 |
| 4 | Tapping temperature ℃ | 300-440 | 300-440 |
Reactor table 5
| Sequence number | Project | R-1 | R-2 |
| 1 | Temperature ℃ | ||
| The initial stage～phase not | 300～440 | 300～440 | |
| Phase at bottom initial stage～not | 290～380 | 290～380 | |
| Phase at regeneration initial stage～not | ＜480 | ＜480 | |
| 2 | Bed temperature drop ℃ | 20～30 | 10～30 |
| 3 | Pressure Mpa (cutting off) | ||
| The top | 0.5-1.0 | 0.3-0.6 | |
| Regeneration | 0.2 | 0.15 | |
| 4 | Bed pressure drop Mpa (cutting off) | 0.03 | 0.03 |
| 5 | Air speed (V) hr- 1 | 0.2-0.8 | 0.2-0.8 |
Tower table 6
| Sequence number | Project | T-1 | T-2 | T-3 | T-4 |
| 1 | Pressure MPa (cutting off) | ||||
| Cat head | 0.8-1.3 | 0.8-1.3 | 0.7-1.2 | 0.8-1.3 | |
| At the bottom of the tower | 0.82-1.33 | 0.83-1.33 | 0.73-1.23 | 0.84-1.33 | |
| 2 | Temperature ℃ | ||||
| Cat head | 30-40 | 55-75 | 30-40 | 50-60 | |
| At the bottom of the tower | 40-50 | 100-130 | 40-50 | 160-180 |
From following table 7, table 8 as can be seen, after above-mentioned technology, the low octane value gasoline research octane number (RON) improves 23-30 unit approximately, satisfies the component of No. 90 motor spirit.
Feedstock property table 7
Product property table 8
Can see that from table 9 process yield of the present invention than higher, is respectively 73%, 88%.
Product distribution table 9
As can be seen from Table 10, the isomery reformulated gasoline is to contain alkene premium component seldom, is in harmonious proportion with the catalytic gasoline component, can solve the too high problem of catalytic gasoline olefin(e) centent.
The group composition table 10 of raw material, product
Claims (8)
1. low octane value gasoline non-hydrogen isomery modifying process, include feed gasoline and be transported to process furnace (F-1) through pump (P-1), enter reactor (R-1), after being transported to stabilizer tower (T-2) end reboiler (E-7) heat exchange, the underflow product that it is characterized in that reactor (R-1) sends into interchanger (E-1) heat exchange again, dereaction product water cooler (E-2) enters catch pot (V-1) and carries out gas-liquid separation then; Separating tank (V-1) underflow product raw gasline is extracted out through pump (P-2) and is delivered to top, absorption tower (T-1), and its top apoblema rich gas goes to bottom, absorption tower (T-1); The top apoblema dry gas on absorption tower (T-1) is discharged; Absorption tower (T-1) underflow product enters stabilizer tower (T-2) middle part after interchanger (E-5) is delivered in column bottoms pump (P-3) extraction, its overhead product enters return tank (V-2) after water cooler (E-6) cooling, its underflow product liquid hydrocarbon is extracted out through pump (P-4), enters stabilizer tower (T-2) top and/or enters the liquid hydrocarbon holding tank; Stabilizer tower (T-2) bottom product isomery reformulated gasoline enters interchanger (E-5), then enters interchanger (E-3), water cooler (E-4) cooling, enters absorption tower (T-1) and pushes up and/or enter isomery reformulated gasoline holding tank.
2. low octane value gasoline non-hydrogen isomery modifying process as claimed in claim 1, its feature also includes the reaction product after reboiler (E-7) heat exchange, and sends into interchanger (E-1) heat exchange after desorption tower (T-3) end reboiler (E-8) heat exchange again; After separating tank (V-1) top apoblema rich gas goes rich gas compressor (C-1) compression, with mix from the stripping gas on desorption tower (T-3) top and/or through the release underflow product rich absorbent oil of self-absorption tower (T-1) of pump (P-3), enter equilibrium vaporization jar (V-3) gas-liquid separation, jar (V-3) top apoblema compression rich gas enters bottom, absorption tower (T-1); Stingy self-absorption tower (T-1) top enters two-level absorption tower (T-4) bottom, and the absorption agent catalytic diesel oil enters top of tower, absorbs diesel oil behind the liquid hydrocarbon and goes out device at the bottom of by tower; Dry gas is discharged from two-level absorption tower (T-4) top; The condensate oil of equilibrium vaporization jar (V-3) is extracted out through fresh feed pump (P-5) and is delivered to interchanger (E-3) heat exchange, enters desorption tower (T-3) top then, and stripping gas advances equilibrium vaporization jar (V-3) from desorption tower (T-3) top; The rich absorbent oil at desorption tower (T-3) end enters stabilizer tower (T-2) middle part after fresh feed pump (P-6) is delivered to interchanger (E-5) heat exchange.
3. low octane value gasoline non-hydrogen isomery modifying process as claimed in claim 1 or 2, it is characterized in that further comprising the respond underflow product of device (R-1) and can be transported to process furnace (F-2), enter reactor (R-2), its underflow product is transported to stabilizer tower (T-2) end reboiler (E-7) heat exchange.
4. low octane value gasoline non-hydrogen isomery modifying process as claimed in claim 3 is characterized in that reaction pressure is 0.1-1.05Mpa; Temperature of reaction is 300-440 ℃; Reaction velocity is 0.2-0.8 (V) hr
-1
5. low octane value gasoline non-hydrogen isomery modifying process as claimed in claim 4 is characterized in that in reactor (R-1), (R-2) catalyzer being arranged, and catalyzer is the molecular sieve catalyst ZSM-5 of remodeling.
6. low octane value gasoline non-hydrogen isomery modifying process as claimed in claim 5 is characterized in that reactor is a fixed bed adiabatic reactor.
7. low octane value gasoline non-hydrogen isomery modifying process as claimed in claim 6 is characterized in that absorption tower (T-1) pressure is 0.08-1.3MPa, and temperature is 30-60 ℃; Stabilizer tower (T-2) reaction pressure is 0.8-1.3MPa, and temperature is 50-180 ℃; Desorption tower (T-3) pressure is 0.8-1.3MPa, and temperature is 60-130 ℃; Two-level absorption tower (T-4) pressure is 0.7-1.3MPa, and temperature is 30-50 ℃.
8. low octane value gasoline non-hydrogen isomery modifying process as claimed in claim 7 is characterized in that feed gasoline includes the recovery lighter hydrocarbons of straight-run spirit, coker gasoline, pressure gasoline, oil-gas field.
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| CNB2003101058340A CN1329487C (en) | 2003-10-09 | 2003-10-09 | Hydrogen free isomerization upgrading process for low bracker gasoline |
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| CNB2003101058340A CN1329487C (en) | 2003-10-09 | 2003-10-09 | Hydrogen free isomerization upgrading process for low bracker gasoline |
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| CN1329487C true CN1329487C (en) | 2007-08-01 |
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| CN101244395B (en) * | 2008-03-11 | 2011-04-27 | 蓝星石化有限公司天津石油化工厂 | Device for regeneration and charring of straight-run gasoline gasoline non-hydro modified catalyst |
| FR3027302B1 (en) * | 2014-10-20 | 2018-01-05 | Axens | PROCESS FOR ISOMERIZING C5 / C6 HYDROCARBON CUTS WITH RECYCLING OF CHLORINATED COMPOUNDS |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4389303A (en) * | 1979-12-12 | 1983-06-21 | Metallgesellschaft Aktiengesellschaft | Process of converting high-boiling crude oils to equivalent petroleum products |
| CN1066870A (en) * | 1992-06-17 | 1992-12-09 | 洛阳市石油化工研究所 | Non-hydro isomerizaiton process |
-
2003
- 2003-10-09 CN CNB2003101058340A patent/CN1329487C/en not_active Expired - Lifetime
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4389303A (en) * | 1979-12-12 | 1983-06-21 | Metallgesellschaft Aktiengesellschaft | Process of converting high-boiling crude oils to equivalent petroleum products |
| CN1066870A (en) * | 1992-06-17 | 1992-12-09 | 洛阳市石油化工研究所 | Non-hydro isomerizaiton process |
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| Publication number | Publication date |
|---|---|
| CN1605616A (en) | 2005-04-13 |
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