CN107987872B - C4 alkylation process for reducing acid consumption - Google Patents

C4 alkylation process for reducing acid consumption Download PDF

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CN107987872B
CN107987872B CN201711112802.1A CN201711112802A CN107987872B CN 107987872 B CN107987872 B CN 107987872B CN 201711112802 A CN201711112802 A CN 201711112802A CN 107987872 B CN107987872 B CN 107987872B
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alkylation
raw material
tower
reactor
water
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CN107987872A (en
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孙柏军
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Panjin Northern Asphalt Fuel Co ltd
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Panjin Northern Asphalt Fuel Co ltd
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    • 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
    • C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
    • 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
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
    • 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
    • C10G2300/1081—Alkanes
    • 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
    • C10G2300/1088—Olefins
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/205—Metal content

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention discloses a C4 alkylation process for reducing acid consumption, which comprises the following steps: (1) feeding the C4 raw material containing sodium ions into a C4/C5 fractionating tower for fractionating to ensure that part of the sodium ions are left at the bottom of the tower, condensing a gas phase into a liquid phase at the top of the tower, then returning part of the liquid phase to the fractionating tower, and discharging part of the liquid phase out of the fractionating tower to obtain an alkylation raw material; (2) the alkylation raw material enters a water washing tower and is washed by forced circulating water and desalted water in sequence, so that the pH value of the alkylation raw material is less than or equal to 7.5; (3) then the alkylation raw material sequentially passes through a diene removal reactor and an alkylation reactor and then enters a fractionation system to respectively obtain alkylate, normal butane and isobutane, and the isobutane is used as a raw material and returns to the alkylation reactor; concentrated sulfuric acid is added in the alkylation reactor, and waste sulfuric acid in the alkylation reactor is discharged out of the alkylation reactor. The process can effectively remove sodium ions in the C4 raw material, effectively reduce the pH value of the C4 raw material to below 7.5, and enable the diene removal reactor to be normally used.

Description

C4 alkylation process for reducing acid consumption
Technical Field
The invention relates to a C4 alkylation process, in particular to a C4 alkylation process for reducing acid consumption.
Background
The conventional flow of a C4 alkylation device is shown in FIG. 2, a C4 raw material 101 enters a water scrubber 102, the water scrubber is used for washing impurities harmful to the alkylation device, such as methanol, alkali and the like, the washed C4 raw material enters a diene removal reactor 103, a small amount of diene in the raw material is converted into mono-olefin under the action of a noble metal catalyst in the reactor, the raw material is formally fed into an alkylation reactor 104 together with part of isobutane 110 separated and returned from a product after pretreatment, the olefin and the isobutane in the C4 raw material are subjected to alkylation reaction under the action of 106 to finally generate the required alkylate 108, meanwhile, waste sulfuric acid 107 is discharged, the reacted product enters a rear fractionation system 105 for separation, so that alkylate 108, normal butane 109 and isobutane 110 are respectively obtained, and the isobutane returns to the raw material.
Because part of C4 raw materials are complex in source and often contain a certain amount of alkali, the pH value in the raw materials is up to 10-11, the Na + content in the raw materials is also high, the pH value of the part of C4 raw materials after being washed by water 102 in a washing tower is still up to more than 8.5, the diene removal reactor 103 in an alkylation device cannot be put into use, the consumption of sulfuric acid in the device is greatly increased, the acid consumption for producing one ton of alkylate oil reaches 110-120 kg, the content of sodium ions in the generated waste acid 107 is high and can reach 50-90 ppm, the sodium ion content is high, the long-period operation of a waste acid regeneration device is difficult, the reason is that the high-sodium waste acid is easy to generate scales during regeneration, the scales block a pipeline of a steam-generating boiler to cause the regeneration device to be incapable of long-period operation, and the shutdown and the scale cleaning are often required to be performed for.
Disclosure of Invention
In order to solve the problem that the consumption of sulfuric acid of a C4 alkylation device is increased due to the fact that a C4 raw material contains alkali, the application provides a C4 alkylation process capable of reducing the consumption of acid, sodium ions in the C4 raw material can be effectively removed by the process, the pH value of the C4 raw material can be effectively reduced to be below 7.5 after the C4 raw material is washed by a water washing tower, and a diene removal reactor can be normally used. The specific technical scheme is as follows:
a C4 alkylation process with reduced acid consumption comprising the following scheme:
(1) feeding the C4 raw material containing sodium ions into a C4/C5 fractionating tower for fractionating, so that part of sodium ions carried by the C4/C3925 raw material are left at the bottom of the fractionating tower, the gas phase is condensed into a liquid phase at the top of the C4/C5 fractionating tower, and then one part of the liquid phase is returned to the C4/C5 fractionating tower for reflux, and the other part of the liquid phase is discharged from the C4/C5 fractionating tower to form an alkylation raw material after sodium ions are removed;
(2) the alkylation raw material after sodium ion removal enters a water washing tower for water washing; in the water washing tower, the alkylation raw material is washed by forced circulating water at the lower part of the water washing tower and then by desalted water at the upper part of the water washing tower, and the pH value of the washed alkylation raw material is less than or equal to 7.5;
(3) the alkylation raw material discharged from the water scrubber sequentially passes through a diene removal reactor and an alkylation reactor and then enters a fractionation system, and the alkylation raw material is fractionated by the fractionation system to respectively obtain alkylate, normal butane and isobutane, wherein the isobutane is used as a raw material and returns to the alkylation reactor;
concentrated sulfuric acid with the concentration of more than or equal to 91 wt% is added in the alkylation reactor, and waste sulfuric acid generated after reaction in the alkylation reactor is discharged out of the alkylation reactor.
In step (1), in the C4/C5 fractionation column, all of the C4 hydrocarbons and a part of the C5 hydrocarbons are withdrawn from the top of the column, and a part of the C5 hydrocarbons and a part of sodium ions remain at the bottom of the column.
In the alkylation reaction system, concentrated sulfuric acid with the concentration of more than or equal to 91 wt% is present, and the concentration of sulfuric acid is reduced after the alkylation reaction is carried out under the action of the concentrated sulfuric acid, so that 98% of new sulfuric acid needs to be supplemented, and a part of sulfuric acid with low concentration needs to be properly discharged, and the part of discharged sulfuric acid is called waste sulfuric acid for short.
In the invention, two processes are added, namely, a raw material fractionation process is added to remove most of metals brought by raw material clamps; and secondly, a forced water washing procedure is additionally arranged to further remove metals and other impurities.
(1) And adding a fractionation process. The fractionating process is carried out by adopting a C4/C5 fractionating tower, in a C4/C5 fractionating tower, a C4 raw material containing sodium ions is fractionated, the sodium ions cannot be vaporized and evaporated, most of the sodium ions are remained at the bottom of the fractionating tower, a small amount of sodium ions can ascend to the top of the fractionating tower along with tiny liquid drops produced by evaporation, a part of the sodium ions ascending to the top of the fractionating tower returns to the bottom of the fractionating tower along with a liquid phase formed after condensation, the other part of the sodium ions is discharged from the C4/C5 fractionating tower along with a gas phase and enters a sodium-removing alkylation raw material after condensation, but the amount of the sodium ions entering the sodium-removing alkylation raw material is very small, most of the sodium ions are remained in a bottom liquid of the C4/C5 fractionating tower, and when the concentration of the sodium ions in the bottom liquid reaches a certain value, the bottom liquid is discharged for recovery treatment.
Further, in the C4/C5 fractionator, all C4 hydrocarbons are removed overhead and C5 hydrocarbons and sodium ions remain at the bottom. In the C4/C5 fractionating tower, the distillation temperature and reflux ratio are controlled, so that all C4 hydrocarbons can be discharged from the top of the tower, a small amount of C5 hydrocarbons are inevitably discharged along with the C4 hydrocarbons in the distillation process, most of C5 hydrocarbons and sodium ions are left at the bottom of the tower, and when the sodium ions are gathered to a certain concentration, the sodium ions are discharged from the bottom of the tower for centralized recovery processing. Most of the C5 hydrocarbon is kept in the C4/C5 fractionating tower, which ensures the purity of the raw material entering the alkylation reactor and ensures the smooth proceeding of the alkylation reaction.
Preferably, the pressure in the C4/C5 fractionating tower is 0.6-0.7 MPa. The bottom temperature of the C4/C5 fractionating tower is 90-100 ℃, and the top temperature is 55-60 ℃. The reflux ratio of the overhead condensate of the C4/C5 fractionating tower is 0.8-1.0.
Under the conditions, the C4/C5 fractionating tower can be stably ensured to be capable of ensuring that C4 hydrocarbon can be gasified and discharged from the tower top while sodium ions are remained at the tower bottom in the operation process, and the reflux of the tower top condensate liquid ensures that most of the gasified C5 hydrocarbon can be liquefied and then returns to the tower bottom, so that the C5 hydrocarbon is prevented from being discharged from the C4/C5 fractionating tower, and further the smooth proceeding of the subsequent alkylation reaction is influenced.
Further, in the present invention, the heat source of the bottom reboiler of the C4/C5 fractionation column was 1.0MPa of steam. The temperature of the 1.0MPa steam is about 185 ℃, and the bottom temperature of the C4/C5 fractionating tower can be stably kept between 90 ℃ and 100 ℃ at the temperature.
(2) And adding a forced water washing tower. Forced circulating water is added at the lower part of the water washing tower for washing, so that even if the pH value of the C4 raw material is high, the requirement that the pH value is less than or equal to 7.5 can be met after the C4 raw material is washed by the tower, and the rear diene removal reactor can be normally put into use.
Specifically, the pressure in the water washing tower is controlled to be 0.95-1.05 MPa; the water quantity of the forced circulation water is 10-15 tons/hour, the water quantity of the desalted water is 3-5 tons/hour, and the tower boundary position of the washing tower is controlled by the discharge quantity of the sewage.
After the C4 raw material is treated by adding two processes, the impurity content after the water washing tower is very low, and the pH value of the sodium-removed alkylation raw material can be ensured to be not higher than 7.5, so that the subsequent production process can be smoothly carried out. In the diene removing reactor, the amount of sodium ions is extremely small, so that the pore channels of the catalyst cannot be blocked, the diene can be smoothly removed, the olefin and the isobutane in the raw materials can be stably alkylated under the action of concentrated sulfuric acid, and the side reaction can be effectively controlled within a set range.
The concentration of sodium ions in the waste sulfuric acid discharged from the alkylation reactor is less than or equal to 15 ppm. In the reaction process, the concentration of sodium ions in the waste sulfuric acid needs to be controlled, when the concentration of the sodium ions in the waste sulfuric acid is too high, the waste acid is easy to form scales when being regenerated, the growth speed of the scales is very high, a pipeline of a steam generation boiler can be blocked in a short time, the downstream waste acid regeneration device stops running, the scales need to be stopped to be treated, the rapid growth of the scales can seriously restrict the long-period running of the waste acid regeneration device, after the concentration of the sodium ions in the waste sulfuric acid is less than or equal to 15ppm, the formation of the scales can be effectively avoided, and the long-period running of the downstream waste acid regeneration device is ensured.
After the method is adopted, the consumption of sulfuric acid can be greatly reduced, the acid consumption for producing one ton of alkylate oil is kept below 70kg, and the concentration of sodium ions in the waste acid is kept at a lower level, so that the generation of scales during waste acid regeneration is avoided, the pipeline smoothness of a steam generating boiler is ensured, the condition that a downstream waste acid regeneration device cannot operate for a long period is further ensured, and the operation efficiency of the whole C4 alkylation and downstream waste acid regeneration device is improved.
Drawings
FIG. 1 is a schematic flow diagram of an embodiment of the present invention.
FIG. 2 is a schematic flow diagram of a prior art alkylation unit.
Reference numerals:
10-C4 raw material, 20-C4/C5 fractionating tower, 30-forced circulating water, 40-desalted water, 50-diene removing reactor, 60-alkylation reactor, 70-fractionating system, 80-concentrated sulfuric acid, 90-waste sulfuric acid, 100-alkylate oil, 120-n-butane, 130-isobutane and 150-external desalted water.
101-C4 raw material, 102-water washing tower, 103-diene removing reactor, 104-alkylation reactor, 105-fractionation system, 106-concentrated sulfuric acid, 107-waste sulfuric acid, 108-alkylate oil, 109-n-butane and 110-isobutane.
Detailed Description
The invention is further described with reference to fig. 1, wherein a reduced acid consumption C4 alkylation process comprises the following steps:
(1) feeding the C4 raw material 10 containing sodium ions into a C4/C5 fractionating tower 20 for fractionating, enabling part of the sodium ions carried by the raw material to remain at the bottom of the tower, condensing a gas phase into a liquid phase at the top of the C4/C5 fractionating tower 20, returning one part of the gas phase to the C4/C5 fractionating tower 20 for reflux, and discharging the other part of the gas phase out of the C4/C5 fractionating tower 20 to form an alkylation raw material after sodium ions are removed.
In the C4/C5 fractionator, all C4 hydrocarbons and a portion of C5 hydrocarbons are removed overhead, and a portion of C5 hydrocarbons and a portion of sodium ions remain at the bottom of the column.
In the embodiment, the pressure in the C4/C5 fractionating tower is 0.6MPa, the temperature at the bottom of the C4/C5 fractionating tower is 90-100 ℃, the temperature at the top of the fractionating tower is 55-60 ℃, and the reflux ratio of the condensate at the top of the C4/C5 fractionating tower is 0.8-1.0.
It is understood that the column internal pressure of the C4/C5 fractionator may be 0.62MPa, 0.64MPa, 0.66MPa, or 0.7MPa, but may be any value between 0.6 and 0.7 MPa.
In the C4/C5 fractionating column 20, sodium ions remain in the bottom liquid during distillation due to their high density, and the bottom liquid is discharged when the concentration of sodium ions in the bottom liquid reaches a certain level. All of the C4 hydrocarbons and a small amount of C5 hydrocarbons are removed overhead from the C4/C5 fractionator 20 as a sodium-ion depleted alkylation feed, and a majority of the C5 hydrocarbons remain at the bottom of the fractionator during the fractionation.
In this example, the heat source for the bottom reboiler of the C4/C5 fractionator was 1.0MPa of steam.
(2) The alkylation raw material after sodium ion removal enters a water washing tower for water washing, in the water washing tower, the alkylation raw material is firstly washed by forced circulating water 30 at the lower part of the water washing tower and then washed by desalted water 40 at the upper part of the water washing tower, and the pH value of the washed alkylation raw material is less than or equal to 7.5;
in the embodiment, the pressure in the water washing tower is controlled to be 0.95-1.05 MPa; the forced circulation water amount is 10-15 tons/hour, the demineralized water amount is 3-5 tons/hour, the tower boundary of the washing tower is controlled by the sewage discharge amount, the demineralized water for washing is supplied by the external demineralized water 150 in order to keep the tower boundary of the washing tower stable, and the sewage discharge amount of the washing tower is approximately the same as the external demineralized water supply amount.
After the two-stage water washing, namely the washing of the forced circulating water of the first stage and the washing of the desalted water of the second stage, even if the pH value of the C4 raw material is higher, after the two-stage water washing, the pH value of the C4 raw material can also meet the requirement of not higher than 7.5, the requirement of the subsequent process is met, and the normal use of the rear diene removal reactor is ensured.
(3) The alkylation raw material discharged from the water scrubber sequentially passes through a diene removal reactor 50 and an alkylation reactor 60 and then enters a fractionation system 70, and is fractionated by the fractionation system 70 to obtain alkylate oil 100, normal butane 120 and isobutane 130, wherein the isobutane 130 is used as a raw material and returns to the alkylation reactor 60;
concentrated sulfuric acid 80 with the concentration of more than or equal to 91 wt% is added in the alkylation reactor 60, and waste sulfuric acid 90 generated after the reaction in the alkylation reactor 60 is discharged out of the alkylation reactor 60.
In this example, the concentration of sodium ions in the spent sulfuric acid exiting the alkylation reactor was 15ppm or less.
In this embodiment, since sodium ions in the C4 raw material are removed in advance, the pressure of the subsequent water washing in the water washing tower is reduced, so that the pH of the sodium-removed alkylation raw material after the secondary water washing can be less than 7.5, and the C4 raw material can smoothly remove dienes in the diene-removing reactor, thereby avoiding the increase of side reactions during the alkylation reaction, and simultaneously ensuring the stability of the sulfuric acid concentration, so that the alkylation reaction can smoothly proceed. Therefore, the olefin and the isobutane in the sodium-removed alkylation raw material added into the alkylation reactor 50 are subjected to efficient reaction under the action of concentrated sulfuric acid, the concentration of sodium ions in the waste sulfuric acid discharged from the alkylation reactor is reduced to be less than or equal to 15ppm, and the long-term operation of a waste acid regeneration device is ensured.
The consumption of sulfuric acid in alkylate was also effectively reduced after reducing the concentration of sodium ions in the C4 feedstock, and in this example, the consumption of sulfuric acid for producing one ton of alkylate was reduced to below 70 kg.

Claims (6)

1. A C4 alkylation process with reduced acid consumption, which is characterized by comprising the following steps:
(1) feeding the C4 raw material containing sodium ions into a C4/C5 fractionating tower for fractionating, so that part of sodium ions carried by the C4/C3925 raw material are left at the bottom of the fractionating tower, the gas phase is condensed into a liquid phase at the top of the C4/C5 fractionating tower, and then one part of the liquid phase is returned to the C4/C5 fractionating tower for reflux, and the other part of the liquid phase is discharged from the C4/C5 fractionating tower to form an alkylation raw material after sodium ions are removed;
(2) the alkylation raw material after sodium ion removal enters a water washing tower for water washing; in the water washing tower, the alkylation raw material is washed by forced circulating water at the lower part of the water washing tower and then by desalted water at the upper part of the water washing tower, and the pH value of the washed alkylation raw material is less than or equal to 7.5;
(3) the alkylation raw material discharged from the water scrubber sequentially passes through a diene removal reactor and an alkylation reactor and then enters a fractionation system, and the alkylation raw material is fractionated by the fractionation system to respectively obtain alkylate, normal butane and isobutane, wherein the isobutane is used as a raw material and returns to the alkylation reactor;
concentrated sulfuric acid with the concentration of more than or equal to 91 wt% is added in the alkylation reactor, and waste sulfuric acid generated after reaction in the alkylation reactor is discharged out of the alkylation reactor;
in the step (1), the reflux ratio of the overhead condensate of the C4/C5 fractionating tower is 0.8-1.0;
the concentration of sodium ions in the waste sulfuric acid discharged from the alkylation reactor is less than or equal to 15 ppm.
2. The C4 alkylation process according to claim 1, wherein the pressure in the water scrubber is controlled to 0.95-1.05 MPa; the water quantity of the forced circulation water is 10-15 tons/hour, the water quantity of the desalted water is 3-5 tons/hour, and the tower boundary position of the washing tower is controlled by the discharge quantity of the sewage.
3. The C4 alkylation process according to claim 1, wherein, in step (1), in the C4/C5 fractionation column, all C4 hydrocarbons and part of C5 hydrocarbons are discharged from the top of the column, and part of C5 hydrocarbons and part of sodium ions remain at the bottom of the column.
4. The C4 alkylation process according to claim 1, wherein, in the step (1), the C4/C5 fractionation tower has an internal pressure of 0.6-0.7 MPa.
5. The C4 alkylation process according to claim 1, wherein, in the step (1), the C4/C5 fractionation tower has a bottom temperature of 90-100 ℃ and a top temperature of 55-60 ℃.
6. The C4 alkylation process of claim 1, wherein, in step (1), the heat source of the bottom reboiler of the C4/C5 fractionation column is 1.0MPa of steam.
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CN1224676C (en) * 2002-09-28 2005-10-26 中国石油化工股份有限公司 Light hydrocarbon distillate selective dediene catalyst and method for preparing the same
US8119848B2 (en) * 2008-10-01 2012-02-21 Catalytic Distillation Technologies Preparation of alkylation feed
CN104151119B (en) * 2014-08-08 2016-01-13 山东利丰达生物科技有限公司 The method of octane-iso is prepared in the deep processing of a kind of carbon four
CN205295237U (en) * 2015-12-17 2016-06-08 陕西华浩轩新能源科技开发有限公司 Sulfuric acid alkylation device
CN106631657B (en) * 2016-12-13 2017-09-19 联力环保新能源股份有限公司 A kind of production line that isooctane is prepared with iso-butane, butene alkylation
CN106927989B (en) * 2017-03-07 2021-05-07 惠州宇新化工有限责任公司 Process method for improving alkylation reaction efficiency and reducing product separation energy consumption

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