CN104560148A - Light gasoline catalytic rectification etherification device and technique - Google Patents
Light gasoline catalytic rectification etherification device and technique Download PDFInfo
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- CN104560148A CN104560148A CN201510042272.2A CN201510042272A CN104560148A CN 104560148 A CN104560148 A CN 104560148A CN 201510042272 A CN201510042272 A CN 201510042272A CN 104560148 A CN104560148 A CN 104560148A
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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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a light gasoline catalytic rectification etherification device and technique. The device comprises a pre-reactor, a catalytic reaction rectification tower, a methanol extraction tower and a methanol refinement tower. The technique comprises the following steps: a light gasoline raw material containing active olefins is mixed with methanol in the pre-reactor to perform etherification reaction so as to generate TAME (tert amyl methyl ether); the reaction product is pumped to the catalytic reaction rectification tower; new methanol is supplemented into the tower, so that the active olefins perform etherification reaction with the methanol, wherein the total conversion rate is 99.5% above; under the rectifying action, the TAME and other heavy components are distilled off from the tower bottom, the unreacted active olefins, methanol and other light components are distilled off from the tower top and enter the methanol extraction tower; and water enters via the upper part of the methanol extraction tower, the methanol water solution is discharged from the tower bottom and enters the methanol refinement tower, the methanol is discharged from the top of the methanol refinement tower and returns to the pre-reactor, and the water from the tower bottom returns to the upper part of the methanol extraction tower, thereby implementing recycling. The method is simple, has the advantages of favorable effect and high conversion rate of active olefins, and is beneficial to lowering the olefin content and enhancing the octane number of the oil product in the field of etherification of light gasoline.
Description
Technical field
The present invention relates to a kind of petroleum naphtha catalytic distillation ether-based device and technique, belong to technical field of petrochemical industry.
Background technology
Along with the reinforcement of environmental consciousness, countries in the world improve constantly the requirement that gasoline combustion discharges.The too high meeting of olefin(e) centent in gasoline causes stabilization of gasoline poor, affect oxygen in gasoline and stabilize index, the easy variable color of oil product, form colloid, easy blocking engine nozzle, in engine intake valve and combustion chamber, generate settling, and the Thorough combustion of gasoline can be affected, the exhaust emission of aggravation vehicle exhaust.In addition, the alkene that volatility is stronger, easy discharge vaporization enters air, accelerates the generation of Tropospheric ozone, forms photo-chemical smog, and therefore reducing catalytic cracking gasoline olefine content is solve the high key of motor spirit olefin(e) centent.
Summary of the invention
Goal of the invention: the object of the invention is to for the deficiencies in the prior art, provides a kind of petroleum naphtha catalytic distillation ether-based device and technique, reduces oil product olefin(e) centent, improves oil product octane value.
Technical scheme: a kind of petroleum naphtha catalytic distillation ether-based device of the present invention, comprises pre-reactor, catalytic rectifying column, methanol extraction tower and refining methanol tower;
Described pre-reactor top is provided with pre-reactor opening for feed, and bottom is provided with pre-reactor discharge port;
Described catalytic rectifying column tower top is provided with catalytic rectifying column tower top discharge port, and top is provided with catalytic rectifying column methanol feeding mouth and catalytic rectifying column opening for feed, is provided with outlet for product after etherificate at the bottom of tower;
Described methanol extraction tower top is provided with supplementary feed opening for feed, and bottom is provided with methanol extraction tower opening for feed, and tower top is provided with methanol extraction column overhead discharge port, is provided with discharge port at the bottom of methanol extraction tower tower at the bottom of tower;
Be provided with refining methanol tower opening for feed in the middle part of described refining methanol tower, tower top is provided with refining methanol column overhead discharge port, is provided with discharge port at the bottom of refining methanol tower tower at the bottom of tower;
The pre-reactor discharge port of described pre-reactor connects the catalytic rectifying column opening for feed of catalytic rectifying column, the catalytic rectifying column tower top discharge port of described catalytic rectifying column connects the methanol extraction tower opening for feed of methanol extraction tower, and at the bottom of the methanol extraction tower tower of described methanol extraction tower, discharge port connects the refining methanol tower opening for feed of refining methanol tower;
The pre-reactor opening for feed on described pre-reactor top be connected with pre-reactor methanol feed line and contain alkene petroleum naphtha feeding line, the refining methanol column overhead discharge port of described refining methanol tower is connected with pre-reactor methanol feed line;
The supplementary feed opening for feed of described methanol extraction tower is connected with supplementary feed feeding line, and at the bottom of the refining methanol tower tower of described refining methanol tower, discharge port is connected with supplementary feed feeding line.
Further, the rectifying section of described catalytic rectifying column and etherification reaction section adopt window diversion type structured packing.
Adopt above-mentioned petroleum naphtha catalytic distillation ether-based device to carry out the technique of petroleum naphtha catalytic distillation etherificate, comprise the steps:
1.1, the petroleum naphtha raw material and methyl alcohol that contain active olefin are entered pre-reactor from pre-reactor opening for feed, active olefin in petroleum naphtha and methyl alcohol carry out preliminary etherification reaction and generate tert amyl methyl ether(TAME) (TAME), the transformation efficiency of active olefin is 90-92%, and reacted mixture is by the extraction of pre-reactor discharge port;
1.2, the mixture of step 1.1 extraction and the new methyl alcohol supplemented are entered in catalytic rectifying column by catalytic rectifying column opening for feed, catalytic rectifying column methanol feeding mouth respectively, there is etherification reaction further and generate TAME in active olefin and methyl alcohol, after twice etherification reaction, active olefin total conversion rate reaches more than 99.5%, through refinery distillation, heavy constituent mixture distillates from outlet for product after etherificate at the bottom of tower, and light constituent mixture distillates from catalytic rectifying column tower top discharge port;
1.3, the light constituent mixture that step 1.2 distillates enters methanol extraction tower by methanol extraction tower opening for feed, water enters methanol extraction tower by supplementary feed opening for feed, after extraction, methanol aqueous solution is from discharge port extraction at the bottom of methanol extraction tower tower, and remaining ingredient is by the extraction of methanol extraction column overhead discharge port;
1.4, the methanol aqueous solution of step 1.3 extraction enters refining methanol tower by refining methanol tower mixture opening for feed, and after fractionation by distillation, methyl alcohol is from the extraction of refining methanol column overhead discharge port, and water is from discharge port extraction at the bottom of refining methanol tower tower;
1.5, the methyl alcohol of extraction in step 1.4 enters pre-reactor by pre-reactor methanol feed line, recycles; The water of extraction enters methanol extraction tower by supplementary feed feeding line and recycles.
Improve technique scheme further, the working temperature of described pre-reactor is 40-80 DEG C, and pre-reactor working pressure is 0.01-0.8MPa.
The theoretical plate number of described catalytic rectifying column is 20-60 block, and working pressure is 0.01-0.5Mpa.
The working pressure of described methanol extraction tower and refining methanol tower is 0.01-0.5Mpa.
Compared with prior art, its beneficial effect is in the present invention:
(1) structural shape of catalytic rectifying column adopts window diversion type structured packing catalyzer, effectively increases gas-liquid mass transfer area, improves gas-liquid mass transfer speed, improve mass-transfer efficiency further.
(2) whole technique and device, achieves the cyclically utilizing of two intermediate chemical: the systemic circulation of extraction agent-water, and in process, loss is less; Methyl alcohol after extraction is through refining methanol tower Posterior circle reuse feed circuit, and raw material material consumption reduces greatly.
(3) the inventive method is simple, effective, transformation efficiency is high, is conducive to reducing olefin(e) centent in Etherification of Light FCC Gasoline field, improving oil product octane value, is an energy-conserving and environment-protective technology, meets industry development relevant policies.
Accompanying drawing explanation
Fig. 1 is the structural representation of petroleum naphtha catalytic distillation ether-based device described in embodiment 1.
Fig. 2 is that catalytic rectifying column packing layer assembly A and assembly B stacks and the vertical view of curling placement.
Fig. 3 to be catalytic rectifying column packing layer assembly A with assembly B be alternately arranged vertical vertical view placed.
Fig. 4 is the center section schematic diagram of Fig. 3.
In figure: 1-pre-reactor, 2-catalytic rectifying column, 3-methanol extraction tower, 4-refining methanol tower, 5-assembly A, 6-assembly B, a-methanol feeding, b-is containing the charging of alkene petroleum naphtha, c-remaining ingredient, the charging of d-supplementary feed, product discharge after e-etherificate, f-supplements methanol feeding.
Embodiment
Below in conjunction with accompanying drawing, technical solution of the present invention is described in detail, but protection scope of the present invention is not limited to described embodiment.
Embodiment 1:
A kind of petroleum naphtha catalytic distillation ether-based device, comprises pre-reactor, catalytic rectifying column, methanol extraction tower and refining methanol tower;
Described pre-reactor top is provided with pre-reactor opening for feed, and bottom is provided with pre-reactor discharge port;
Described catalytic rectifying column tower top is provided with catalytic rectifying column tower top discharge port, and top is provided with catalytic rectifying column methanol feeding mouth and catalytic rectifying column opening for feed, is provided with outlet for product after etherificate at the bottom of tower;
The rectifying section of described catalytic rectifying column and etherification reaction section adopt window diversion type structured packing, assembly A and the assembly B of two kinds of different structures is comprised in every layer of packing layer, assembly A be window diversion packing sheet external parcel silk screen, in fill out ion exchange resin and fill catalyzer, assembly B is structured packing sheet, assembly A and assembly B stacks and curling, then fix with banding sheet, form catalytic rectification packing, as shown in Figure 2.
As replacement, assembly A and assembly B also can be alternately arranged vertical placement in every layer of packing layer, as shown in Figures 3 and 4.
Described methanol extraction tower top is provided with supplementary feed opening for feed, and bottom is provided with methanol extraction tower opening for feed, and tower top is provided with methanol extraction column overhead discharge port, is provided with discharge port at the bottom of methanol extraction tower tower at the bottom of tower;
Be provided with refining methanol tower opening for feed in the middle part of described refining methanol tower, tower top is provided with refining methanol column overhead discharge port, is provided with discharge port at the bottom of refining methanol tower tower at the bottom of tower;
The pre-reactor discharge port of described pre-reactor connects the catalytic rectifying column opening for feed of catalytic rectifying column, the catalytic rectifying column tower top discharge port of described catalytic rectifying column connects the methanol extraction tower opening for feed of methanol extraction tower, and at the bottom of the methanol extraction tower tower of described methanol extraction tower, discharge port connects the refining methanol tower opening for feed of refining methanol tower;
The pre-reactor opening for feed on described pre-reactor top be connected with pre-reactor methanol feed line and contain alkene petroleum naphtha feeding line, the refining methanol column overhead discharge port of described refining methanol tower is connected with pre-reactor methanol feed line;
The supplementary feed opening for feed of described methanol extraction tower is connected with supplementary feed feeding line, and at the bottom of the refining methanol tower tower of described refining methanol tower, discharge port is connected with supplementary feed feeding line.
In the present embodiment, the processing step adopting said apparatus to carry out petroleum naphtha catalytic distillation etherificate is:
1.1, will (main component be 2-methyl-1-butene alkene containing active olefin, 2-methyl-2-butene) petroleum naphtha raw material and methyl alcohol enter pre-reactor from pre-reactor opening for feed, carry out etherification reaction and generate TAME, wherein: methyl alcohol is 6.73 × 10 to the feed flow rates of pre-reactor
3kg/h, petroleum naphtha is 4.42 × 10 to the feed flow rates of pre-reactor
4kg/h, pre-reactor temperature is 50 DEG C, and pre-reactor working pressure is 0.1MPa, and reacted mixture is by the extraction of pre-reactor discharge port.
1.2, the mixture of step 1.1 extraction and the new methyl alcohol supplemented are entered in catalytic rectifying column by catalytic rectifying column methanol feeding mouth, catalytic rectifying column opening for feed respectively, there is etherification reaction further and generate TAME in active olefin and methyl alcohol, through refinery distillation, heavy constituent mixture distillates from outlet for product after etherificate at the bottom of tower, described heavy constituent mixture comprises TAME etc., and light constituent mixture distillates from catalytic rectifying column tower top discharge port; Light constituent mixture comprises unreacted active olefin and methyl alcohol etc.
The stage number of catalytic rectifying column is 38 blocks of (rectifying section column plates 2nd ~ 6 pieces, catalyst reaction section column plate 7th ~ 26 pieces, stripping section column plate 27th ~ 37 pieces), supplement feed entrance point the 7th block of column plate of methyl alcohol, feed entrance point the 27th block of column plate of the mixture of step 1.1 extraction.
Supplementary methyl alcohol is 760kg/h to the feed flow rates of catalytic rectifying column, and the working pressure of catalytic rectifying column is 0.3Mpa.
1.3, the light constituent mixture that step 1.2 distillates enters methanol extraction tower by methanol extraction tower opening for feed, water enters methanol extraction tower by supplementary feed opening for feed, countercurrent exchange is carried out with water, after extraction, methanol aqueous solution is from discharge port extraction at the bottom of methanol extraction tower tower, remaining ingredient is by the extraction of methanol extraction column overhead discharge port, and remaining ingredient is mainly unreacted active olefin.
Water is 1.80 × 10 to the feed flow rates of methanol extraction tower
3kg/h, the stage number of methanol extraction tower is 4 pieces, and working pressure is 0.1Mpa.
1.4, the methanol aqueous solution of step 1.3 extraction enters refining methanol tower by refining methanol tower mixture opening for feed, and after fractionation by distillation, methyl alcohol is from the extraction of refining methanol column overhead discharge port, and water is from discharge port extraction at the bottom of refining methanol tower tower; Stage number in refining methanol tower is 10 pieces, and the methanol solution of extraction phase enters from the 9th block of column plate, and working pressure is 0.1Mpa.
1.5, in step 1.4, the methyl alcohol of extraction meets after methanol feedstock requires after testing, enters pre-reactor, recycle by pre-reactor methanol feed line; The water of extraction enters methanol extraction tower by supplementary feed feeding line and recycles.
Pre-reactor, catalytic rectifying column, material between methanol extraction tower and refining methanol tower pass through pump delivery.
In pre-reactor, the total conversion rate of 2-methyl-1-butene alkene and 2-methyl-2-butene is 90.6%, and after catalytic distillation reaction, the total conversion rate of 2-methyl-1-butene alkene and 2-methyl-2-butene is 99.7%; After etherification reaction, the methyl alcohol of gasoline and the content of alkene are respectively 0.3% and 11.0% (massfraction).
Table 1: the methyl alcohol liquid phase flow rate of extraction phase and recycle after extraction at the bottom of petroleum naphtha charging in embodiment 1, pre-reactor discharge port, catalytic rectifying column overhead extraction and tower, extraction and composition
Embodiment 2:
The petroleum naphtha catalytic distillation ether-based device adopted in the present embodiment, identical with embodiment 1.
In the present embodiment, the processing step adopting said apparatus to carry out petroleum naphtha catalytic distillation etherificate is:
1.1, will (main component be 2-methyl-1-butene alkene containing active olefin, 2-methyl-2-butene) petroleum naphtha raw material and methyl alcohol enter pre-reactor from pre-reactor opening for feed, carry out preliminary etherification reaction and generate TAME, wherein: methyl alcohol is 6.44 × 10 to the feed flow rates of pre-reactor
3kg/h, petroleum naphtha is 5.00 × 10 to the feed flow rates of pre-reactor
4kg/h, pre-reactor temperature is 60 DEG C, and pre-reactor working pressure is 0.1MPa, and reacted mixture is by the extraction of pre-reactor discharge port.
1.2, the mixture of step 1.1 extraction and the new methyl alcohol supplemented are entered in catalytic rectifying column by catalytic rectifying column methanol feeding mouth, catalytic rectifying column opening for feed respectively, there is etherification reaction further and generate TAME in active olefin and methyl alcohol, through refinery distillation, heavy constituent mixture distillates from outlet for product after etherificate at the bottom of tower, described heavy constituent mixture comprises TAME, and light constituent mixture distillates from catalytic rectifying column tower top discharge port; Light constituent mixture comprises unreacted active olefin and methyl alcohol.
The stage number of catalytic rectifying column is 40 blocks of (rectifying section column plates 2nd ~ 8 pieces, catalyst reaction section column plate 9th ~ 29 pieces, stripping section column plate 30th ~ 39 pieces), supplement feed entrance point the 9th block of column plate of methyl alcohol, feed entrance point the 27th block of column plate of the mixture of step 1.1 extraction.
Supplementary methyl alcohol is 112.56kg/h to the feed flow rates of catalytic rectifying column, and the working pressure of catalytic rectifying column is 0.35Mpa.
1.3, the light constituent mixture that step 1.2 distillates enters methanol extraction tower by methanol extraction tower opening for feed, water enters methanol extraction tower by supplementary feed opening for feed, countercurrent exchange is carried out with water, after extraction, methanol aqueous solution is from discharge port extraction at the bottom of methanol extraction tower tower, remaining ingredient is by the extraction of methanol extraction column overhead discharge port, and remaining ingredient is mainly unreacted active olefin.
Water is 1.08 × 10 to the feed flow rates of methanol extraction tower
3kg/h, the stage number of methanol extraction tower is 6 pieces, and working pressure is 0.3Mpa.
1.4, the methanol aqueous solution of step 1.3 extraction enters refining methanol tower by refining methanol tower mixture opening for feed, and after fractionation by distillation, methyl alcohol is from the extraction of refining methanol column overhead discharge port, and water is from discharge port extraction at the bottom of refining methanol tower tower; Stage number in refining methanol tower is 14 pieces, and the methanol solution of extraction phase enters from the 13rd block of column plate, and working pressure is 0.3Mpa.
1.5, in step 1.4, the methyl alcohol of extraction meets after methanol feedstock requires after testing, enters pre-reactor, recycle by pre-reactor methanol feed line; The water of extraction enters methanol extraction tower by supplementary feed feeding line and recycles.
Pre-reactor, catalytic rectifying column, material between methanol extraction tower and refining methanol tower pass through pump delivery.
In pre-reactor, the total conversion rate of 2-methyl-1-butene alkene and 2-methyl-2-butene is 90.3%, and after catalytic distillation reaction, the total conversion rate of 2-methyl-1-butene alkene and 2-methyl-2-butene is 99.6%; After ether, the methyl alcohol of gasoline and the content of alkene are respectively 0.3% and 14.8% (massfraction).
Table 2: petroleum naphtha charging in embodiment 2, pre-reactor discharging, catalytic rectifying column tower top and the extraction of tower reactor liquid phase, the methyl alcohol liquid phase flow rate extracting rear extraction phase and recycle and composition
Embodiment 3:
The petroleum naphtha catalytic distillation ether-based device adopted in the present embodiment, identical with embodiment 1.
In the present embodiment, the processing step adopting said apparatus to carry out petroleum naphtha catalytic distillation etherificate is:
1.1, will (main component be 2-methyl-1-butene alkene containing active olefin, 2-methyl-2-butene) petroleum naphtha raw material and methyl alcohol enter pre-reactor from pre-reactor opening for feed, carry out preliminary etherification reaction and generate TAME, wherein: methyl alcohol is 9.06 × 10 to the feed flow rates of pre-reactor
3kg/h, petroleum naphtha is 6.00 × 10 to the feed flow rates of pre-reactor
4kg/h, pre-reactor temperature is 45 DEG C, and pre-reactor working pressure is 0.1MPa, and reacted mixture is by the extraction of pre-reactor discharge port.
1.2, the mixture of step 1.1 extraction and the new methyl alcohol supplemented are entered in catalytic rectifying column by catalytic rectifying column methanol feeding mouth, catalytic rectifying column opening for feed respectively, there is etherification reaction further and generate TAME in active olefin and methyl alcohol, through refinery distillation, heavy constituent mixture distillates from outlet for product after etherificate at the bottom of tower, described heavy constituent mixture comprises TAME, and light constituent mixture distillates from catalytic rectifying column tower top discharge port; Light constituent mixture comprises unreacted active olefin and methyl alcohol.
The stage number of catalytic rectifying column is 50 blocks of (rectifying section column plates 2nd ~ 6 pieces, catalyst reaction section column plate 7th ~ 38 pieces, stripping section column plate 39th ~ 49 pieces), supplement feed entrance point the 7th block of column plate of methyl alcohol, feed entrance point the 44th block of column plate of the mixture of step 1.1 extraction.
Supplementary methyl alcohol is 5.16 × 10 to the feed flow rates of catalytic rectifying column
3kg/h, the working pressure of catalytic rectifying column is 0.3Mpa.
1.3, the light constituent mixture that step 1.2 distillates enters methanol extraction tower by methanol extraction tower opening for feed, water enters methanol extraction tower by supplementary feed opening for feed, countercurrent exchange is carried out with water, after extraction, methanol aqueous solution is from discharge port extraction at the bottom of methanol extraction tower tower, remaining ingredient is by the extraction of methanol extraction column overhead discharge port, and remaining ingredient is mainly unreacted active olefin.
Water is 5.40 × 10 to the feed flow rates of methanol extraction tower
3kg/h, the stage number of methanol extraction tower is 2 pieces, and working pressure is 0.1Mpa.
1.4, the methanol aqueous solution of step 1.3 extraction enters refining methanol tower by refining methanol tower mixture opening for feed, and after fractionation by distillation, methyl alcohol is from the extraction of refining methanol column overhead discharge port, and water is from discharge port extraction at the bottom of refining methanol tower tower; Stage number in refining methanol tower is 20 pieces, and the methanol solution of extraction phase enters from the 19th block of column plate, and working pressure is 0.1Mpa.
1.5, in step 1.4, the methyl alcohol of extraction meets after methanol feedstock requires after testing, enters pre-reactor, recycle by pre-reactor methanol feed line; The water of extraction enters methanol extraction tower by supplementary feed feeding line and recycles.
Pre-reactor, catalytic rectifying column, material between methanol extraction tower and refining methanol tower pass through pump delivery.
In pre-reactor, the total conversion rate of 2-methyl-1-butene alkene and 2-methyl-2-butene is 91.2%, and after urging rectification process, the total conversion rate of 2-methyl-1-butene alkene and 2-methyl-2-butene is 99.5%; After ether, the methyl alcohol of gasoline and the content of alkene are respectively 0.04% and 8.97% (massfraction).
Table 3: petroleum naphtha charging in embodiment 3, pre-reactor discharging, catalytic rectifying column tower top and the extraction of tower reactor liquid phase, the methyl alcohol liquid phase flow rate extracting rear extraction phase and recycle and composition
As mentioned above, although represented with reference to specific preferred embodiment and described the present invention, it shall not be construed as the restriction to the present invention self.Under the spirit and scope of the present invention prerequisite not departing from claims definition, various change can be made in the form and details to it.
Claims (6)
1. a petroleum naphtha catalytic distillation ether-based device, is characterized in that: comprise pre-reactor, catalytic rectifying column, methanol extraction tower and refining methanol tower;
Described pre-reactor top is provided with pre-reactor opening for feed, and bottom is provided with pre-reactor discharge port;
Described catalytic rectifying column tower top is provided with catalytic rectifying column tower top discharge port, and top is provided with catalytic rectifying column methanol feeding mouth and catalytic rectifying column opening for feed, is provided with outlet for product after etherificate at the bottom of tower;
Described methanol extraction tower top is provided with supplementary feed opening for feed, and bottom is provided with methanol extraction tower opening for feed, and tower top is provided with methanol extraction column overhead discharge port, is provided with discharge port at the bottom of methanol extraction tower tower at the bottom of tower;
Be provided with refining methanol tower opening for feed in the middle part of described refining methanol tower, tower top is provided with refining methanol column overhead discharge port, is provided with discharge port at the bottom of refining methanol tower tower at the bottom of tower;
The pre-reactor discharge port of described pre-reactor connects the catalytic rectifying column opening for feed of catalytic rectifying column, the catalytic rectifying column tower top discharge port of described catalytic rectifying column connects the methanol extraction tower opening for feed of methanol extraction tower, and at the bottom of the methanol extraction tower tower of described methanol extraction tower, discharge port connects the refining methanol tower opening for feed of refining methanol tower;
The pre-reactor opening for feed on described pre-reactor top be connected with pre-reactor methanol feed line and contain alkene petroleum naphtha feeding line, the refining methanol column overhead discharge port of described refining methanol tower is connected with pre-reactor methanol feed line;
The supplementary feed opening for feed of described methanol extraction tower is connected with supplementary feed feeding line, and at the bottom of the refining methanol tower tower of described refining methanol tower, discharge port is connected with supplementary feed feeding line.
2. petroleum naphtha catalytic distillation ether-based device according to claim 1, is characterized in that, the rectifying section of described catalytic rectifying column and etherification reaction section adopt window diversion type structured packing.
3. adopt the petroleum naphtha catalytic distillation ether-based device described in claim 1 or 2 to carry out the technique of petroleum naphtha catalytic distillation etherificate, it is characterized in that, comprise the steps:
1.1, the petroleum naphtha raw material and methyl alcohol that contain active olefin are entered pre-reactor by pre-reactor opening for feed, carry out preliminary etherification reaction, reacted mixture is by the extraction of pre-reactor discharge port;
1.2, the mixture of step 1.1 extraction and the new methyl alcohol supplemented are entered in catalytic rectifying column by catalytic rectifying column opening for feed, catalytic rectifying column methanol feeding mouth respectively, there is etherification reaction further in active olefin and methyl alcohol, through refinery distillation, heavy constituent mixture distillates from outlet for product after etherificate at the bottom of tower, and light constituent mixture distillates from catalytic rectifying column tower top discharge port;
1.3, the light constituent mixture that step 1.2 distillates enters methanol extraction tower by methanol extraction tower opening for feed, water enters methanol extraction tower by supplementary feed opening for feed, after extraction, methanol aqueous solution is from discharge port extraction at the bottom of methanol extraction tower tower, and remaining ingredient is by the extraction of methanol extraction column overhead discharge port;
1.4, the methanol aqueous solution of step 1.3 extraction enters refining methanol tower by refining methanol tower mixture opening for feed, and after fractionation by distillation, methyl alcohol is from the extraction of refining methanol column overhead discharge port, and water is from discharge port extraction at the bottom of refining methanol tower tower;
1.5, the methyl alcohol of extraction in step 1.4 enters pre-reactor by pre-reactor methanol feed line, recycles; The water of extraction enters methanol extraction tower by supplementary feed feeding line and recycles.
4. the technique of petroleum naphtha catalytic distillation etherificate according to claim 3, is characterized in that, the working temperature of described pre-reactor is 40-80 DEG C, and pre-reactor working pressure is 0.01-0.8MPa.
5. the technique of petroleum naphtha catalytic distillation etherificate according to claim 3, is characterized in that, the theoretical plate number of described catalytic rectifying column is 20-60 block, and working pressure is 0.01-0.5Mpa.
6. the technique of petroleum naphtha catalytic distillation etherificate according to claim 3, it is characterized in that, the working pressure of methanol extraction tower and refining methanol tower is 0.01-0.5Mpa.
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Cited By (2)
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