CN205774350U - A kind of environmentally friendly solvent and partial monosomy alkane process units - Google Patents
A kind of environmentally friendly solvent and partial monosomy alkane process units Download PDFInfo
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- CN205774350U CN205774350U CN201620669280.XU CN201620669280U CN205774350U CN 205774350 U CN205774350 U CN 205774350U CN 201620669280 U CN201620669280 U CN 201620669280U CN 205774350 U CN205774350 U CN 205774350U
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Abstract
nullThis utility model provides a kind of environmentally friendly solvent and partial monosomy alkane process units，Its technical scheme is: main by feed pump (1)、Heat exchanger package (2)、Circulating hydrogen compressor (3)、New hydrogen line (4)、De-lighter hydrocarbons tower (5)、Heating furnace (6)、Pre-hydrogenator (7)、Main hydrogenation reactor (8)、Adsorptive reactor (9)、First takes off arylation reaction device (10)、Second takes off arylation reaction device (11)、High-pressure separator (12)、Low pressure separator (13)、Pentane rectifying column (14)、Hexane rectifying column (15)、Heptane rectifying column one (16)、Heptane rectifying column two (17)、Hydrogenation tail oil rectifying column (18)、Isohexane rectifying column (19)、N-hexane extraction rectifying column (20)、First extractant recovery tower (21)、Methyl cyclopentane rectifying column (22)、Second extractant recovery tower (23)、Benzene rectifying column (24)、First extractant regeneration vaporizer (25) and the second extractant regeneration vaporizer (26) are constituted；This utility model practicality reasonable in design, better economic benefit.
Description
Technical field:
This utility model relates to solvent naphtha technical field, and especially a kind of environmentally friendly solvent and partial monosomy alkane produce dress
Put.
Background technology:
China's existing petroleum hydrocarbon solvent process units and method generally are directed to raw material sources and product standard at that time
Being designed, so existence processes raw material limited, product quality poor (Volatile organic emissions is high, and abnormal smells from the patient is big), device adds
The problems such as work very flexible, can not meet the demand for development of current environmentally friendly solvent.Petroleum hydrocarbon solvent produces the most both at home and abroad
Technology mainly has extraction fractional distillation, adsorption method of separation, sulfonation method and a catalytic hydrogenation method, wherein catalytic hydrogenation method be apply the widest
General method.Catalytic hydrogenation method solvent naphtha produces and includes cut and refined two processes.Catalytic hydrogenation plant investment compares
Greatly, noble metal catalyst is expensive, is not suitable for medium-sized and small enterprises investment construction.Sulfonation method is limited because of the waste pollution environment of generation
System.So urgently researching and developing new preparation facilities and production method, playing low pressure hydrofining and producing high-end with solvent extraction
The comprehensive advantage of solvent product, to meet the application needs of environmentally friendly solvent, solves current China and is short of high-end high-purity ring the most in a large number
The problem protecting solvent.Hydrofinishing method mainly depends on the consideration of device operation pressure, temperature and catalyst input cost at present.?
On the premise of ensureing selectivity of catalyst, select low-valent metal catalyst can be substantially reduced catalyst cost, the most permissible
Reduce reaction pressure and reaction temperature, reduce hydrogen consumption.Inevitable the combining with rectification of hydrofinishing just can obtain high purity product.Commonly
Rectification method can not get high-purity monomer alkane product；Molecular sieve adsorption is the most saturated, regeneration difficulty；Extraction fractional distillation is possible not only to
Obtaining the product of higher degree, production cost is relatively low simultaneously, is usually used in aromatic hydrocarbons and separates with non-aromatics.For extraction fractional distillation
For the selection of extractant extremely important, extractant that we commonly use include N-Methyl pyrrolidone, glycols, sulfolane,
Dimethyl sulfoxide, N-formyl-morpholine etc..Relative between feed change component of extractant and the mass ratio of raw material (solvent than)
Volatility has a major impact；Extractant has a major impact for extraction efficiency with the mass transfer area of raw material.In certain opereating specification
In, solvent ratio is the biggest, and the effect of extract and separate is the best, but with the increase of solvent ratio, the consumption of extractant can increase, cause energy
Consumption and the increase of cost.By using new packing extraction tower to increase extraction tower inner transmission matter area, improve extraction efficiency, effectively subtract
Few solvent consumption caused than increase because of solvent.Therefore, the selection of catalyst, the process technique of extractant and extraction tower design are right
Operating cost and the efficiency of device have a major impact.
Summary of the invention
The purpose of this utility model is to overcome above-mentioned deficiency, it is provided that a kind of environmentally friendly solvent and partial monosomy alkane coproduction dress
Put, particularly to pentane, normal hexane, hexane, petroleum ether, heptane, benzene, dimethylbenzene and state V light oil constituents from extractant in process
Circulation and refined a kind of environmentally friendly solvent and partial monosomy alkane process units, its technical scheme is: feed pump, heat exchanger
Group, de-lighter hydrocarbons tower are sequentially connected and connect, and new hydrogen line one end connects de-lighter hydrocarbons tower, and the other end connects circulating hydrogen compressor, heating furnace one
Side lower part connects de-lighter hydrocarbons tower, and opposite side top connects pre-hydrogenator, the pre-hydrogenator of reactor unit, main hydrogenation
Reactor, adsorptive reactor, first taking off arylation reaction device, second take off arylation reaction device and be sequentially connected and connect, high-pressure separator side connects
Heat exchanger package, top connects circulating hydrogen compressor, and bottom connects low pressure separator, main hydrogenation reactor, low pressure separator and essence
Evaporate the pentane rectifying column of unit, hexane rectifying column, heptane rectifying column one, heptane rectifying column two, hydrogenation tail oil rectifying column phase successively
Connect, pentane rectifying column bottom outlet two and the isohexane rectifying column of rectification extraction cells, the n-hexane extraction of rectification cell
Rectifying column, the first extractant recovery tower, methyl cyclopentane rectifying column, the second extractant recovery tower, benzene rectifying column are sequentially connected and connect,
First extractant recovery tower and the second extractant recovery tower are respectively equipped with the first extractant regeneration vaporizer and the second extractant again
Raw vaporizer, n-hexane extraction rectifying column, the first extractant recovery tower and the first extractant regeneration vaporizer form loop, methyl
Pentamethylene. rectifying column, the second extractant recovery tower and the second extractant regeneration vaporizer form loop.
The beneficial effects of the utility model: practicality reasonable in design, hydrogen consumption, energy consumption are low, and operation pressure is low, and rectification purity is high,
Three waste discharge is few, technological operation simple and flexible, and product is in addition to state V light oil, and low sulfur and low aromatics, purity is high, adapts to current environmental protection molten
Agent raw material is uncertain strong, the diversified requirement of the market demand, better economic benefit.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Detailed description of the invention
As it is shown in figure 1, a kind of environmentally friendly solvent and partial monosomy alkane process units, mainly by feed pump 1, heat exchanger package 2,
Circulating hydrogen compressor 3, new hydrogen line 4, de-lighter hydrocarbons tower 5, heating furnace 6, pre-hydrogenator 7, main hydrogenation reactor 8, adsorption reaction
Device 9, first take off arylation reaction device 10, second take off arylation reaction device 11, high-pressure separator 12, low pressure separator 13, pentane rectifying column 14,
Hexane rectifying column 15, heptane rectifying column 1, heptane rectifying column 2 17, hydrogenation tail oil rectifying column 18, isohexane rectifying column 19, just
Hexane extractive distillation column the 20, first extractant recovery tower 21, methyl cyclopentane rectifying column the 22, second extractant recovery tower 23, benzene
Rectifying column the 24, first extractant regeneration vaporizer 25 and the second extractant regeneration vaporizer 26 are constituted；Feed pump 1, heat exchanger package
2, de-lighter hydrocarbons tower 5 is sequentially connected and connects, and new hydrogen line 4 one end connects de-lighter hydrocarbons tower 5, and the other end connects circulating hydrogen compressor 3, heating furnace
6 one side lower parts connect de-lighter hydrocarbons towers 5, and opposite side top connects pre-hydrogenator 7, the pre-hydrogenator 7 of reactor unit,
Main hydrogenation reactor 8, adsorptive reactor 9, first taking off arylation reaction device 10, second take off arylation reaction device 11 and be sequentially connected and connect, high pressure divides
Connect heat exchanger package 2 from device 12 side, top connects circulating hydrogen compressor 3, and bottom connects low pressure separator 13, main hydrogenation reaction
Device 8, low pressure separator 13 and the pentane rectifying column 14 of rectification cell, hexane rectifying column 15, heptane rectifying column 1, heptane rectification
Tower 2 17, hydrogenation tail oil rectifying column 18 are sequentially connected and connect, and pentane rectifying column 14 bottom outlet two of rectification cell extracts with rectification
Take the isohexane rectifying column 19 of unit, n-hexane extraction rectifying column the 20, first extractant recovery tower 21, methyl cyclopentane rectifying column
22, the second extractant recovery tower 23, benzene rectifying column 24 are sequentially connected and connect, and the first extractant recovery tower 21 and the second extractant reclaim
Tower 23 is respectively equipped with the first extractant regeneration vaporizer 25 and the second extractant regeneration vaporizer 26, n-hexane extraction rectifying column
20, the first extractant recovery tower 21 and the first extractant regeneration vaporizer 25 form loop, methyl cyclopentane rectifying column 22, second
Extractant recovery tower 23 and the second extractant regeneration vaporizer 26 form loop.
This utility model technological process: first carry out alkali cleaning pretreatment according to naphtha cut feedstock property, by raw material
Sulfur content is down to below 2500ppm.Raw material enters after feed pump 1 pumps into heat exchanger package 2 heat exchange de-lighter hydrocarbons tower 5, and removing is light
The material of component is carried out new hydrogen with circulating hydrogen compressor 3 recycle hydrogen with new hydrogen line 4 before heating furnace 6 and is mixed, and enters heating furnace 6 and heats up
After sequentially pass through the pre-hydrogenator 7 of reactor unit, main hydrogenation reactor 8, adsorptive reactor 9, first take off arylation reaction device
10, second takes off that arylation reaction device 11 carries out secondary hydrogenation, absorption, secondary take off arylation reaction, enters height after reactant heat exchanger package 2 heat exchange
Pressure separator 12, isolated hydrogen compresses through circulating hydrogen compressor 3 and again recycles, and the material after dehydrogenation divides through low pressure
Enter rectification cell or rectification extraction cells from device 13, cut rectification accordingly according to product boiling range and can get environmentally friendly solvent
Product and part high-purity monomer alkane.Through rectification cell, pentane foaming agent can be obtained, each board with hexane, heptane as main component
Number environmentally friendly solvent and petroleum ether, lightweight white oil etc., hydrogenation tail oil can obtain high boiling solvent and state V light oil through rectification.Enter rectification
The material of extraction cells can obtain high-purity normal hexane, isohexane, methyl cyclopentane, benzene, dimethylbenzene equal solvent through rectification, extraction.
Five-pointed star ring aluminum silicon protective agent preferable particle size 19.0mm in pre-hydrogenator 7, the gear ring nickel preferred grain of molybdenum protective agent
Footpath 10.0mm, Raschig ring nickel molybdenum catalyst preferable particle size 6.0mm, the preferential particle diameter of reactor bottom is 6.0mm Yu 13.0mm porcelain ball
Backing supports.The porcelain ball of the catalyst of three kinds of shapes and two kinds of particle diameters preferentially presses the volume of 4:8:73:3:3 by order described above
Ratio loads.
Five-pointed star ring aluminum silicon protective agent preferable particle size 19.0mm in main hydrogenation reactor 8, the gear ring nickel preferred grain of molybdenum protective agent
Footpath 10.0mm, Raschig ring nickel molybdenum catalyst preferable particle size 6.0mm, Herba Trifolii Pratentis nickel molybdenum catalyst preferable particle size 1.6mm, at the bottom of reactor
The preferential particle diameter in portion is that 3.0mm, 6.0mm support with 13.0mm porcelain ball backing.The catalyst of four kinds of shapes and the porcelain ball of three kinds of particle diameters
Preferentially load by the volume ratio of 4:4:12:75:3:3:3 by order described above.
First takes off preferential porcelain ball particle diameter 13.0mm, 6.0mm porcelain ball, the preferential particle diameter of spherical dearomatization catalyst in arylation reaction device 10
2-4mm, preferential porcelain ball particle diameter 6.0mm, preferential porcelain ball particle diameter 6.0mm, spherical dearomatization catalyst preferential particle diameter 2-4mm, preferential porcelain
Spherolite footpath 6.0mm, preferential porcelain ball particle diameter 13.0mm.Catalyst and porcelain ball preferentially press 3:2:22:2:2:22 by order described above:
The volume ratio of 2:2 is loaded.
Second takes off preferential porcelain ball particle diameter 13.0mm, 6.0mm porcelain ball, the preferential particle diameter of spherical dearomatization catalyst in arylation reaction device 11
2-4mm, preferential porcelain ball particle diameter 6.0mm, preferential porcelain ball particle diameter 6.0mm, spherical dearomatization catalyst preferential particle diameter 2-4mm, preferential porcelain
Spherolite footpath 6.0mm, preferential porcelain ball particle diameter 13.0mm.Catalyst and porcelain ball preferentially press 3:2:34:2:2:34 by order described above:
The volume ratio of 2:2 is loaded.
Embodiment 1
Entering de-lighter hydrocarbons tower after raw material pumps into heat exchanger package heat exchange, heated stove is warmed up to 135 DEG C and enters reaction member
Carry out deep hydrodesulfurizationof reaction, denitrogenation, dechlorination reaction and de-virtue saturated reaction；Product is entered height and is added separator gas-liquid and divide
From, the hydrogen-rich gas of gained is recycle hydrogen, and the liquid fraction of gained enters distillation system through low pressure separator, isolates each
The solvent naphtha product of fraction section.Through rectification cell, go out pentane foaming agent product and 30-60 DEG C of petroleum ether in pentane rectifying column rectification
Product；The 6# plant extraction solvent with hexane as main component and 60-90 DEG C of petroleum ether product is gone out in hexane rectifying column rectification；?
Heptane rectifying column one rectification goes out the 120# rubber industry solvent with heptane as main component and 90-120 DEG C of petroleum ether product；?
Heptane rectifying column two rectification goes out 120-160 DEG C of W2-20 lightweight white oil；It is light that tail oil hydrogenated tail oil rectifying column rectification can obtain state V
Oil.In addition to state V light oil, products obtained therefrom is without sulfur, and arene content is extremely low, meets that environmentally friendly solvent abnormal smells from the patient is little, Volatile organic emissions
Low requirement.
Embodiment 2
Entering de-lighter hydrocarbons tower after raw material pumps into heat exchanger package heat exchange, heated stove is warmed up to 145 DEG C and enters reaction member
Carry out deep hydrodesulfurizationof reaction, denitrogenation, dechlorination reaction and de-virtue saturated reaction；Product is entered height and is added separator gas-liquid and divide
From, the hydrogen-rich gas of gained is recycle hydrogen, and the liquid fraction of gained enters distillation system through low pressure separator, isolates each
The solvent naphtha product of fraction section.Through rectification cell, go out pentane foaming agent product and 30-60 DEG C of petroleum ether in pentane rectifying column rectification
Product；The 6# plant extraction solvent with hexane as main component and 60-90 DEG C of petroleum ether product is gone out in hexane rectifying column rectification；?
Heptane rectifying column one rectification goes out the 120# rubber industry solvent with heptane as main component and 90-120 DEG C of petroleum ether product；?
Heptane rectifying column two rectification goes out 20# paint industry solvent and 120-160 DEG C of W2-20 lightweight white oil；135-170 DEG C of W2-30 is light
Matter white oil, 155-200 DEG C of W2-40 lightweight white oil, 185-225 DEG C of W2-60 lightweight white oil, 195-235 DEG C of W2-70 lightweight white oil,
The high boiling points such as 205-245 DEG C of W2-80 lightweight white oil, 215-255 DEG C of W2-90 lightweight white oil, 230-270 DEG C of W2-100 lightweight white oil
Solvent, hydrogenation tail oil can obtain state V light oil through rectification.In addition to state V light oil, products obtained therefrom is without sulfur, and arene content is extremely low, meets ring
Protect the requirement that solvent odor is little, Volatile organic emissions is low.
Embodiment 3
Directly mixing with hydrogen without de-lighter hydrocarbons tower after raw material pumps into heat exchanger package heat exchange, heated stove is warmed up to 125 DEG C
Enter reaction member and carry out deep hydrodesulfurizationof reaction, denitrogenation, dechlorination reaction and de-virtue saturated reaction；Product is entered height and is added
Separator gas-liquid separation, the hydrogen-rich gas of gained is recycle hydrogen, and the liquid fraction of gained enters rectification system through low pressure separator
System, isolates the solvent naphtha product of each fraction section.Through rectification cell, pentane rectifying column rectification go out pentane foaming agent product and
30-60 DEG C of petroleum ether product；The 6# plant extraction solvent with hexane as main component and 60-90 DEG C is gone out in hexane rectifying column rectification
Petroleum ether product；The 120# rubber industry solvent with heptane as main component and 90-120 DEG C is gone out in heptane rectifying column one rectification
Petroleum ether product；120-160 DEG C of W2-20 lightweight white oil is gone out in heptane rectifying column two rectification；Tail oil hydrogenated tail oil rectifying column essence
Evaporate and can obtain state V light oil.In addition to state V light oil, products obtained therefrom is without sulfur, and arene content is extremely low, meet environmentally friendly solvent abnormal smells from the patient little, volatilization
The requirement that property organic emission is low.
Embodiment 4
Directly mixing with hydrogen without de-lighter hydrocarbons tower after raw material pumps into heat exchanger package heat exchange, heated stove is warmed up to 155 DEG C
Enter reaction member and carry out deep hydrodesulfurizationof reaction, denitrogenation, dechlorination reaction and de-virtue saturated reaction；Product is entered height and is added
Separator gas-liquid separation, the hydrogen-rich gas of gained is recycle hydrogen, and the liquid fraction of gained enters rectification system through low pressure separator
System, isolates the solvent naphtha product of each fraction section.Through rectification cell, pentane rectifying column rectification go out pentane foaming agent product and
30-60 DEG C of petroleum ether product；The 6# plant extraction solvent with hexane as main component and 60-90 DEG C is gone out in hexane rectifying column rectification
Petroleum ether product；The 120# rubber industry solvent with heptane as main component and 90-120 DEG C is gone out in heptane rectifying column one rectification
Petroleum ether product；120-160 DEG C of W2-20 lightweight white oil is gone out in heptane rectifying column two rectification；Tail oil hydrogenated tail oil rectifying column essence
Evaporate and can obtain state V light oil.In addition to state V light oil, products obtained therefrom is without sulfur, and arene content is extremely low, meet environmentally friendly solvent abnormal smells from the patient little, volatilization
The requirement that property organic emission is low.
Embodiment 5
Above example gained 6# plant extraction solvent fraction is pumped into rectification extraction cells, extracts through rectification, dissident can be obtained
The products such as alkane, methyl cyclopentane, mixed xylenes and high-purity normal hexane, benzene.Gained normal hexane product purity up to more than 99%,
Other products is without sulfur, and arene content is extremely low, meets the requirement that environmentally friendly solvent abnormal smells from the patient is little, Volatile organic emissions is low.
Claims (1)
1. an environmentally friendly solvent and partial monosomy alkane process units, it is characterised in that: feed pump (1), heat exchanger package (2), de-
Lighter hydrocarbons tower (5) is sequentially connected and connects, and new hydrogen line (4) one end connects de-lighter hydrocarbons tower (5), and the other end connects circulating hydrogen compressor (3), adds
Hot stove (6) side lower part connects de-lighter hydrocarbons tower (5), and opposite side top connects pre-hydrogenator (7), the pre-add of reactor unit
Hydrogen reactor (7), main hydrogenation reactor (8), adsorptive reactor (9), first take off arylation reaction device (10), second take off arylation reaction device
(11) being sequentially connected and connect, high-pressure separator (12) side connects heat exchanger package (2), and top connects circulating hydrogen compressor (3), bottom
Connect low pressure separator (13), the pentane rectifying column (14) of main hydrogenation reactor (8), low pressure separator (13) and rectification cell,
Hexane rectifying column (15), heptane rectifying column one (16), heptane rectifying column two (17), hydrogenation tail oil rectifying column (18) are sequentially connected
Connect, the isohexane rectifying column (19) of pentane rectifying column (14) bottom outlet of rectification cell two and rectification extraction cells, just oneself
Alkane extractive distillation column (20), the first extractant recovery tower (21), methyl cyclopentane rectifying column (22), the second extractant recovery tower
(23), benzene rectifying column (24) be sequentially connected and connect, the first extractant recovery tower (21) and the second extractant recovery tower (23) set respectively
There are the first extractant regeneration vaporizer (25) and a second extractant regeneration vaporizer (26), n-hexane extraction rectifying column (20),
One extractant recovery tower (21) and the first extractant regeneration vaporizer (25) form loop, methyl cyclopentane rectifying column (22), the
Two extractant recovery towers (23) form loop with the second extractant regeneration vaporizer (26).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201620669280.XU CN205774350U (en) | 2016-06-30 | 2016-06-30 | A kind of environmentally friendly solvent and partial monosomy alkane process units |
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| CN201620669280.XU CN205774350U (en) | 2016-06-30 | 2016-06-30 | A kind of environmentally friendly solvent and partial monosomy alkane process units |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950213A (en) * | 2016-06-30 | 2016-09-21 | 东营市俊源石油技术开发有限公司 | Environment-friendly solvent and partial monomer alkane production device and use method thereof |
| CN110105921A (en) * | 2019-04-28 | 2019-08-09 | 东营市俊源石油技术开发有限公司 | A kind of tasteless environment-friendly aerial fog propellant production equipment and production method |
| CN112225633A (en) * | 2020-10-29 | 2021-01-15 | 洛阳金达石化有限责任公司 | Production method of normal hexane containing heptane raw material |
-
2016
- 2016-06-30 CN CN201620669280.XU patent/CN205774350U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950213A (en) * | 2016-06-30 | 2016-09-21 | 东营市俊源石油技术开发有限公司 | Environment-friendly solvent and partial monomer alkane production device and use method thereof |
| CN110105921A (en) * | 2019-04-28 | 2019-08-09 | 东营市俊源石油技术开发有限公司 | A kind of tasteless environment-friendly aerial fog propellant production equipment and production method |
| CN110105921B (en) * | 2019-04-28 | 2022-02-22 | 东营市俊源石油技术开发有限公司 | Production equipment and production method of odorless environment-friendly aerosol propellant |
| CN112225633A (en) * | 2020-10-29 | 2021-01-15 | 洛阳金达石化有限责任公司 | Production method of normal hexane containing heptane raw material |
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