CN109161399B - A kind of liquid hydrocarbon composition containing isoparaffin component - Google Patents
A kind of liquid hydrocarbon composition containing isoparaffin component Download PDFInfo
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- CN109161399B CN109161399B CN201811181777.7A CN201811181777A CN109161399B CN 109161399 B CN109161399 B CN 109161399B CN 201811181777 A CN201811181777 A CN 201811181777A CN 109161399 B CN109161399 B CN 109161399B
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- isoparaffin
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- alkane
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- hydrocarbon composition
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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
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
Abstract
The present invention relates to a kind of liquid hydrocarbon composition containing isoparaffin component.Liquid hydrocarbon composition is prepared by raw material by pretreatment, adsorbing separation, fractionation process, isoparaffin raffinate from adsorptive separation technology is passed through isoparaffin knockout tower first by fractionation process, enter isoparaffin side stripper from isoparaffin knockout tower side line tower tray extract stream, stripper tower bottom obtains 61 DEG C of flash-point > of the liquid hydrocarbon composition containing isoparaffin component.Simple production process of the present invention, yield is high, and low energy consumption.Isoparaffin purity is high is free of cycloalkane, and arene content is low, boiling range is narrow.
Description
Technical field
The invention belongs to ICL for Indirect Coal Liquefaction fields, and in particular to the liquid hydrocarbon composition containing isoparaffin component.
Background technique
Isoparaffin possesses stronger solvability, and has the features such as colourless, tasteless, nontoxic, in aerosol, punching press
The industries such as oil, cleaning, paint, ink have wide application.Wherein, isoparaffin of the flash-point greater than 61 DEG C is particularly suitable for metal
Processing, cleaning, coating, polyolefin synthesize carrier, and peroxide carrier field, the market demand is big, and is not belonging to the United Nations
Combustible liquids object in " proposed standard about danger conveying provides " and " danger ship transports and storage regulation "
Matter is not belonging to dangerous material, convenient transportation.
Isoparaffin currently on the market mostlys come from the Isopar series of the Exxon Mobil of import and Japan goes out light
IP series.Although the isoparaffin purity for the IP series that the Isopar series of Exxon Mobil and Japan go out light is higher,
Wherein contain cycloalkane, it is larger to human body and environmental hazard, and influence performance.
Mobil Oil Corporation (CN1279708A) discloses through F- T synthesis, Fischer Tropsch waxes hydroisomerization and catalysis
The combination of hydrodewaxing step makes the natural gas of low value be converted to High Quality Lube Base Oils, and obtained lube base oil mainly contains
Having normal boiling point is 370 DEG C of isoparaffin component, and it is nitrogenous that liquid hydrocarbon composition contains 0.1% aromatic hydrocarbons of <, < 20pppm W
The cycloalkane of compound, < 20ppm W sulfur-containing compound and low concentration.But the process is more complicated, it is at high cost, and product
Impurity content is also higher.
Sinopec Group (CN101921621B) discloses a kind of production of isoparaffin solvent oil
Method, feedstock oil include vacuum distillate or solvent refining deasphalted oil, and raw material and hydrogen initially enter hydrotreating reaction area
Hydrotreating is carried out, hydrotreatment products carry out gas-liquid separation, the hydrotreating content of wax that obtained liquid phase is sulphur, nitrogen content is very low
Oil is mixed into hygrogenating isomerization reaction area, hydroisomerizing reaction effluent with hydrogen using the hydrotreating waxy oil as raw material
It is directly entered hydrofining reaction zone, further removes alkene and aromatic hydrocarbon impurities；Hydrofining reaction zone reaction stream
For object through gas-liquid separation, product liquid obtains the isoparaffin solvent oil product of various fraction ranges after rectifying out.The original of use
Cycloalkane and arene content are high in material, and the isoparaffin solvent oil product boiling range range of production is wide, and purity is low, and arene content reaches
0.05%.
East China University of Science (CN102585887A) discloses the method for naphtha adsorbing separation, obtained rich in it is non-just
The desolventizing of structure hydrocarbon inhales excess oil, and the content of non-normal hydrocarbons is 90%-100%, and non-normal hydrocarbons includes isoparaffin, cycloalkane and virtue
Hydrocarbon.
Domestic enterprise's isoparaffin production capacity is poor, and yield is small, and purity is low, and universal arene content it is higher (≤
0.1%), big to human body and environmental hazard.
Fischer-Tropsch synthetic usually contains a small amount of cycloalkane, contains in the Fischer-Tropsch synthesis oil as disclosed in CN105505347A few
In the cycloalkane of 10% 9 to 20 carbon atoms；Fisher-Tropsch derived gas and oil disclosed in CN106255740A contains 0-2wt% range
Cycloalkane.
It produces in the raw material of high-purity isoparaffin and production technology and final products performance is all had not containing cycloalkane
The influence of benefit.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of flash-points of high-purity to contain isoparaffin group greater than 61 DEG C
The liquid hydrocarbon composition divided, yield is big, and purity and arene content are reached the international leading level, and is free of cycloalkane, harmless.
Cycloalkane is free of in the raw material of use, simple production process, molecular sieve adsorption efficiency is high, and system energy consumption is low.
The technical solution of the present invention is as follows:
A kind of liquid hydrocarbon composition containing isoparaffin component, liquid hydrocarbon composition by raw material by pretreatment,
Adsorbing separation, fractionation process are prepared, and the isoparaffin raffinate from adsorptive separation technology is passed through by fractionation process first
Isoparaffin knockout tower enters isoparaffin side stripper, stripper from isoparaffin knockout tower side line tower tray extract stream
Tower bottom obtains 61 DEG C of flash-point > of the liquid hydrocarbon composition containing isoparaffin component.
Isoparaffin side stripper stripped overhead steam returns to isoparaffin knockout tower.
Normal paraffin content is lower than 2% in isoparaffin raffinate, the tower top pressure 0.08- of isoparaffin knockout tower
0.11MPa, tower bottom pressure 0.12-0.15MPa, 198-210 DEG C of tower top temperature, 270-290 DEG C of column bottom temperature.
The tower top pressure 0.09-0.12MPa of isoparaffin side stripper, tower bottom pressure 0.10-0.13MPa, tower top temperature
200-220 DEG C, 205-225 DEG C of column bottom temperature of degree.
Into isoparaffin side stripper stream by the 5th, 9,15 layer of isoparaffin knockout tower side line tower tray middle and upper part
It is extracted out at three.Using isoparaffin side stripper, 61 DEG C of flash-point > of the liquid hydrocarbon group containing isoparaffin component is obtained
Closing object, low energy consumption, and yield is big, and the product market demand is big.
Adsorbing separation be molecular sieve adsorbing separation, 176-180 DEG C of technological temperature, pressure 2.2-2.5MPa.
Raw material includes the first Fischer-Tropsch crude liquid wax, the second Fischer-Tropsch crude liquid wax, third Fischer-Tropsch crude liquid wax and/or the 4th Fischer-Tropsch crude liquid
Wax.
In raw material, C5-C9 n-alkane: C5-C9 isoparaffin=(2-5): 1, preferably 3: 1, C10-C13 n-alkane
: C10-C13 isoparaffin=(0.8-1): 1, preferably 0.9: 1, C14-C16 n-alkane: C14-C16 isoparaffin=(1-
1.2): 1, preferably 1.1: 1, C17+ n-alkane: C17+ isoparaffin=(1-1.2): 1, preferably 1.1: 1.Control positive structure
The ratio of alkane and isoparaffin can be improved molecular sieve adsorption efficiency within the above range, improve isoparaffin product purity and
Yield.Cycloalkane is free of in raw material, n-alkane and isoparaffin ratio are suitable for that the molecular sieve service life is long.
Other than the ratio of control n-alkane and isoparaffin, in molecular sieve absorption process, molecular sieve void volume
Ratio with n-alkane volume in raw material is preferably 1.15-1.55.
Pretreatment is de- light, the de- weight of weight-removing column of lightness-removing column, the tower top pressure 0.01-0.05MPa of lightness-removing column, tower bottom pressure
0.02-0.06MPa, 155-165 DEG C of tower top temperature, 210-230 DEG C of column bottom temperature.
The tower top pressure 9-13KPa of weight-removing column, tower bottom pressure 15-25KPa, 110-130 DEG C of tower top temperature, column bottom temperature
220-250℃。
Through detecting, cycloalkane is not included in the liquid hydrocarbon composition containing isoparaffin component that the present invention obtains, is evaporated
175-220 DEG C of journey, preferably 180-215 DEG C, further preferably 195-210 DEG C, 84-87 DEG C of aniline point, preferably 85-86,
61 DEG C of arene content < 50ppm, flash-point >.The content > 95% of isoparaffin, preferably > 97% in liquid hydrocarbon composition, into
One step preferred > 98%, still more preferably > 99%.Wherein, the isoparaffin accounting that carbon number is 10 is 5-10%, preferably
6-9%, the isoparaffin that carbon number is 10 are 2- methylnonane, and the isoparaffin accounting that carbon number is 11 is 15-50%, preferably
20-35%, the isoparaffin accounting that carbon number is 12 is 40-75%, preferably 55-70%.The main chain carbon number of isoparaffin is 6-
16, branch carbon number is 1-6.50-95% branch is located at No. 2 carbon, and 5-50% branch is located at No. 3 carbon.Methyl accounting 50- in branch
95%.Isoparaffin isomerisation degree of the invention is high, good product quality.
The present invention pointedly produces the isoparaffin of high-purity being readily transported according to the market demand.Production technology letter
Single, yield is high, and low energy consumption.Isoparaffin purity is high is free of cycloalkane, and arene content is low, boiling range is narrow.
Specific embodiment
Technical solution of the present invention and its effect are described further below by way of specific embodiment.
Raw material is pre-processed, preprocessing process includes that lightness-removing column is de- light, the de- weight of weight-removing column, the tower top pressure of lightness-removing column
0.01-0.05MPa, tower bottom pressure 0.02-0.06MPa, 155-165 DEG C of tower top temperature, 210-230 DEG C of column bottom temperature；Weight-removing column
Tower top pressure 9-13KPa, tower bottom pressure 15-25KPa, 110-130 DEG C of tower top temperature, 220-250 DEG C of column bottom temperature.By de-
Gently, the raw material of Tuo Chonghou enters molecular sieve adsorption separation device, in molecular sieve absorbing process, molecular sieve material feeding temperature 176-
180 DEG C, adsorption chamber bottom pressure 2.2-2.5MPa, 176-180 DEG C of desorbing agent feeding temperature, 176-180 DEG C of flushing liquor feeding temperature,
176-180 DEG C of room temperature of absorption.Isoparaffin raffinate after molecular sieve absorption is passed through isoparaffin knockout tower, and isoparaffin is taken out
Normal paraffin content is lower than 2% in extraction raffinate, the tower top pressure 0.08-0.11MPa of isoparaffin knockout tower, tower bottom pressure 0.12-
0.15MPa, 198-210 DEG C of tower top temperature, 270-290 DEG C of column bottom temperature.From isoparaffin knockout tower side line tower tray middle and upper part
5, extract stream enters isoparaffin side stripper at 9,15 layer three, and stripped overhead steam returns to isoparaffin knockout tower, vapour
Stripper tower bottom obtains 61 DEG C of flash-point > of the liquid hydrocarbon composition containing isoparaffin component.Isoparaffin side stripper
Tower top pressure 0.09-0.12MPa, tower bottom pressure 0.10-0.13MPa, 200-220 DEG C of tower top temperature, column bottom temperature 205-225
℃。
Raw material includes the first Fischer-Tropsch crude liquid wax, the second Fischer-Tropsch crude liquid wax, third Fischer-Tropsch crude liquid wax and/or the 4th Fischer-Tropsch crude liquid
Wax.
First Fischer-Tropsch crude liquid wax accounting 15-35% does not include cycloalkane, the first Fischer-Tropsch crude liquid wax in the first Fischer-Tropsch crude liquid wax
C5-C9 n-alkane including 5-15%, the C5-C9 isoparaffin of 0.1-0.5%, the C10-C13 n-alkane of 35-60%,
The C10-C13 isoparaffin of 1-5%, the C14-C16 n-alkane of 15-40%, the C14-C16 isoparaffin of 1-5%, 5-20%
C17+ n-alkane, the C17+ isoparaffin of 1-5%.
Second Fischer-Tropsch crude liquid wax accounting 15-35% does not include cycloalkane, the second Fischer-Tropsch crude liquid wax in the second Fischer-Tropsch crude liquid wax
C5-C9 n-alkane including 7-16%, the C5-C9 isoparaffin of 0.1-0.6%, the C10-C13 n-alkane of 40-60%,
The C10-C13 isoparaffin of 1-4%, the C14-C16 n-alkane of 20-30%, the C14-C16 isoparaffin of 0.5-3%, 8-
15% C17+ n-alkane, the C17+ isoparaffin of 0.8-2%.
Third Fischer-Tropsch crude liquid wax accounting 35-55% does not include cycloalkane, third Fischer-Tropsch crude liquid wax in third Fischer-Tropsch crude liquid wax
C5-C9 n-alkane including 0.5-2.5%, the C5-C9 isoparaffin of 1-5%, the C10-C13 n-alkane of 3-10%, 40-
60% C10-C13 isoparaffin, the C14-C16 n-alkane of 1-5%, the C14-C16 isoparaffin of 15-25%, 3-6%'s
C17+ n-alkane, the C17+ isoparaffin of 8-15%.
4th Fischer-Tropsch crude liquid wax accounting 3-10% does not include cycloalkane, the 4th Fischer-Tropsch crude liquid wax in the 4th Fischer-Tropsch crude liquid wax
C5-C9 n-alkane including 0.2-0.8%, the C5-C9 isoparaffin of 0.3-1%, the C10-C13 n-alkane of 2-10%,
The C10-C13 isoparaffin of 40-55%, the C14-C16 n-alkane of 2-4%, the C14-C16 isoparaffin of 20-30%, 2-
5% C17+ n-alkane, the C17+ isoparaffin of 9-13%.
In raw material, C5-C9 n-alkane accounting 4-10%, C5-C9 isoparaffin accounting 1-5%, C10-C13 n-alkane
Accounting 15-40%, C10-C13 isoparaffin accounting 20-35%, C14-C16 n-alkane accounting 8-20%, C14-C16 isomery
Alkane accounting 5-20%, C17+ n-alkane accounting 4-10%, C17+ isoparaffin accounting 3-9%.
C5-C9 n-alkane: C5-C9 isoparaffin=(2-5): 1, C10-C13 n-alkane: C10-C13 isoparaffin
=(0.8-1): 1, C14-C16 n-alkane: C14-C16 isoparaffin=(1-1.2): 1, C17+ n-alkane: C17+ isomery
Alkane=(1-1.2): 1.In molecular sieve absorption process, the ratio of n-alkane volume is preferred in molecular sieve void volume and raw material
For 1.15-1.55.
In raw material, control arene content≤20ppm, oxygen content≤1ppm, water content≤40ppm, nitrogen content≤0.3ppm,
Sulfur content≤1ppm, chlorinity≤5ppm, bromine index≤20mgBr/100g, carbonyls≤2ppm.
Embodiment
Liquid hydrocarbon composition containing isoparaffin component is produced using raw material of the present invention and technique.Raw material includes first
Fischer-Tropsch crude liquid wax, the second Fischer-Tropsch crude liquid wax, third Fischer-Tropsch crude liquid wax and the 4th Fischer-Tropsch crude liquid wax.First Fischer-Tropsch crude liquid wax accounting
22.916%, it does not include cycloalkane in the first Fischer-Tropsch crude liquid wax, the first Fischer-Tropsch crude liquid wax includes the 9.066962% positive structure of C5-C9
Alkane, 0.201892% C5-C9 isoparaffin, 47.46498% C10-C13 n-alkane, 2.015039% C10-
C13 isoparaffin, 26.1817% C14-C16 n-alkane, 1.764391% C14-C16 isoparaffin, 12.06655%
C17+ n-alkane, 1.238479% C17+ isoparaffin.Second Fischer-Tropsch crude liquid wax accounting 23.1972%, the second Fischer-Tropsch
It does not include cycloalkane in crude liquid wax, the second Fischer-Tropsch crude liquid wax includes 10.7984425% C5-C9 n-alkane, and 0.265891%
C5-C9 isoparaffin, 47.73631% C10-C13 n-alkane, 2.036661% C10-C13 isoparaffin,
24.9543185% C14-C16 n-alkane, 1.6702325% C14-C16 isoparaffin, 11.340289% C17+
N-alkane, 1.197856% C17+ isoparaffin.Third Fischer-Tropsch crude liquid wax accounting 48.4981438%, third Fischer-Tropsch crude liquid
It does not include cycloalkane in wax, third Fischer-Tropsch crude liquid wax includes 1.406952% C5-C9 n-alkane, 3.011406% C5-
C9 isoparaffin, 6.751762% C10-C13 n-alkane, 50.70609% C10-C13 isoparaffin, 2.557149%
C14-C16 n-alkane, 19.287335% C14-C16 isoparaffin, 4.406087% C17+ n-alkane,
11.791942% C17+ isoparaffin.4th Fischer-Tropsch crude liquid wax accounting 5.3886826% is not wrapped in the 4th Fischer-Tropsch crude liquid wax
Cycloalkane is included, the 4th Fischer-Tropsch crude liquid wax includes 0.530731% C5-C9 n-alkane, 0.684781% C5-C9 isomeric alkane
Hydrocarbon, 6.930366% C10-C13 n-alkane, 49.828965% C10-C13 isoparaffin, 2.597583% C14-
C16 n-alkane, 23.525523% C14-C16 isoparaffin, 3.960207% C17+ n-alkane, 11.857043%
C17+ isoparaffin.
In raw material, C5-C9 n-alkane accounting 5.3%, C5-C9 isoparaffin accounting 1.6%, C10-C13 n-alkane
Accounting 25.6%, C10-C13 isoparaffin accounting 28.2%, C14-C16 n-alkane accounting 13.2%, C14-C16 isomeric alkane
Hydrocarbon accounting 11.4%, C17+ n-alkane accounting 7.7%, C17+ isoparaffin accounting 6.9%.
C5-C9 n-alkane: isoparaffin=3.3 C5-C9: 1, C10-C13 n-alkane: C10-C13 isoparaffin=
0.9: 1, C14-C16 n-alkane: isoparaffin=1.15 C14-C16: 1, C17+ n-alkane: isoparaffin=1.1 C17+:
1。
The tower top pressure 0.03MPa of lightness-removing column, tower bottom pressure 0.04MPa, 161.2 DEG C of tower top temperature, column bottom temperature 220.9
℃。
The tower top pressure 11KPa of weight-removing column, tower bottom pressure 20KPa, 120.9 DEG C of tower top temperature, 230 DEG C of column bottom temperature.
177 DEG C of molecular sieve absorbing process temperature, pressure 2.4MPa.
The tower top pressure 0.1MPa of isoparaffin knockout tower, tower bottom pressure 0.12MPa, 201.6 DEG C of tower top temperature, tower bottom temperature
273.8 DEG C of degree.
The tower top pressure 0.105MPa of isoparaffin side stripper, tower bottom pressure 0.11MPa, 217.9 DEG C of tower top temperature,
219.2 DEG C of column bottom temperature.
Detailed process is as follows:
Raw material exchanges heat through raw material-weight-removing column overhead heat exchanger (E-105AB) to 116 DEG C, into raw material-light component from tank field
Fractionation column top gas heat exchanger (E-115AB) exchanges heat to 136 DEG C, changes into raw material-heavy constituent fractionating column top heat exchanger (E-106)
Heat exchanges heat into raw material-lightness-removing column base oil heat exchanger (E-119AB) to 165 DEG C and enters lightness-removing column (C-101) to 203 DEG C.
C-101 tower overhead gas is through desorbing agent-lightness-removing column top heat exchanger (E-101AB), lightness-removing column tower top air cooler (AC-102)
140 DEG C are cooled to, into lightness-removing column return tank (V-102), tank deck uses the sealed tower top pressure processed of nitrogen, and tank bottom oil is light with taking off
Tower reflux pump (P-102AB) a part is squeezed at the top of lightness-removing column, and a part removes light component fractionating column (C-103) as charging.
It is heated using road oil generation at lightness-removing column bottom reboiler (E-102).Lightness-removing column base oil pumps (P- through lightness-removing column bottom
After 103AB) pressurizeing, by raw material-lightness-removing column base oil heat exchanger (E-119AB), molecular sieve charging-lightness-removing column base oil heat exchanger
(E-120AB) enter weight-removing column (C-102) after exchanging heat.
Weight-removing column (C-102) tower overhead gas is cooled to 40 DEG C through weight-removing column top condenser (E-104), returns into weight-removing column
It flows tank (V-103), tank deck fixed gas connects vacuum pump set, controls tower top pressure at 11KPa (A).Tank bottom oil weight-removing column reflux pump
(P-104AB) it squeezes at the top of weight-removing column.It is heated using road oil generation at weight-removing column bottom reboiler (E-103AB).Weight-removing column base oil
Enter heavy constituent fractionating column (C-104) after weight-removing column bottom pump (P-105AB) pressurization.Molecular sieve charging is taken out from weight-removing column middle and upper part
Out, pump (P-106AB) pressurization tri- tunnel Hou Fen is followed through weight-removing column top, enters withdrawn position lower part all the way, as interior reflux, a part
Enter weight-removing column after air cooler (AC-101ABCD) heat exchange is followed on raw material-weight-removing column overhead heat exchanger (E-105AB), weight-removing column top
Tower top walks around to streamline as tower top, finally all the way after molecular sieve charging-lightness-removing column base oil heat exchanger (E-120AB) heat exchange
Into molecular sieve feed surge tank (V-207).
Light component fractionating column (C-103) tower overhead gas is through raw material-light component fractionation column top gas heat exchanger (E-115AB), light
Component fractionation column overhead air cooler (AC-103) is cooled to 80 DEG C, into light component fractionating column return tank (V-104), tank deck
Using the sealed tower top pressure processed of nitrogen, tank bottom oil is squeezed into light component with light component fractionating column reflux pump (P-111AB) a part and is fractionated
Top of tower, a part are beaten after W2-20 lightweight white oil cooler (E-116AB) is cooling to tank field.Light component fractionating column boils again
Device (E-114) is heated using road oil generation.Light component fractionating column base oil is pressurizeed through light component fractionating column column bottoms pump (P-110AB)
Afterwards, cooling by low temperature hot oil-W2-40 lightweight white oil heat exchanger (E-117AB), W2-40 lightweight white oil cooler (E-118AB)
After beat to tank field.
Heavy constituent fractionating column (C-104) tower overhead gas is through raw material-heavy constituent fractionating column top heat exchanger (E-106), heavy constituent point
It evaporates the column overhead air cooler (AC-105AB) that goes into operation and is cooled to 60 DEG C, into heavy constituent fractionating column return tank (V-105), tank deck
Fixed gas connects vacuum pump set, controls tower top pressure at 11KPa (A).Tank bottom oil heavy constituent fractionating column reflux pump (P-109AB) one
It is partially driven at the top of heavy constituent fractionating column, a part is sent after W2-110 lightweight white oil cooler (E-111AB) is cooling to tank
Area.Heavy constituent Fractionator Bottom reboiler (E-107AB) is heated using road oil generation.Heavy constituent fractionating column base oil is through heavy constituent point
It evaporates after tower column bottoms pump (P-108AB) pressurizes through Extract -5# technical white oil heat exchanger (E-112AB), low-temperature circulating.Hot oil -5#
Tank field is pressed onto after technical white oil heat exchanger (E-110AB), 5# technical white oil cooler (E-113AB) are cooling.Side line is from weight-removing column
Middle part extraction, into white oil side stripper (C-105), tower overhead gas returns to heavy constituent fractionating column (C-104).White oil side line stripping
Tower reboiler (E-121) is heated using road oil generation.White oil side stripper base oil is through W2-140 lightweight white oil drawing pump (P-
It 107AB) pressurizes, through Extract-W2-140 lightweight white oil heat exchanger (E-108AB), W2-140 lightweight white oil cooler (E-
109AB) send as product W2-140 to tank field.
The material of molecular sieve feed surge tank by feed pump (P-204AB) boost after through molecular sieve feed heater (E-
205) 177 DEG C are heated to, then absorption is entered to revolving valve ME-201 by flowmeter by charge filter (FIL-201AB)
Tower.Adsorption tower using adsorbent in charging n-alkane and isoparaffin separate, n-alkane is adsorbed by adsorbent
Afterwards, it is desorbed using desorbing agent, obtains the Extract being made of n-alkane and the raffinate being made of isoparaffin, desorbing agent；
Desorbing agent is the mixture of a kind of 60% pentane and 40% isooctane.For the first time when going into operation, from tank field in proportion to
Desorbing agent compensator V-204 charging.During normal production, it is supplemented to raffinate column from pumping, is converged with raffinate column charging in proportion
Into column plate.It distillates the desorbing agent compensator V-204 after condensation is cooling from raffinate column, Extract tower and desorbing agent tower top.
Desorbing agent in tank is gone out successively to take one's place heat through desorbing agent-Extract tower top heat exchanger (E-225), desorbing agent-lightness-removing column by pumping
Device (E-101AB), desorbing agent-steam tower top heat exchanger (E-218) again, desorbing agent heater (E-207) is heated to 177 DEG C, then leads to
It crosses desorbing agent filter (FIL-202) and enters adsorption tower to revolving valve ME-201 by flowmeter.
Extract is flowed out from adsorption tower enters Extract tower charging blending tank (V-206) through revolving valve and flowmeter.Extraction
Liquid removes Extract flash tank (V- through discharge control valve decompression after multiple injectors in V-206 inlet manifold are uniformly mixed
215) it is flashed, tank deck gas enters Extract tower (C-202), and tank bottom liquid is passed through respectively by being divided into three bursts of logistics after pump pressurization
Extract-IP60 isoparaffin heat exchanger (E-223AB), Extract-W2-140 lightweight white oil heat exchanger (E-108AB), extraction
It merges into one material after liquid -5# technical white oil heat exchanger (E-112AB) heat exchange and enters back into Extract-and steam tower top heat exchanger again
(E-217) enter Extract tower (C-202) after exchanging heat and carry out rectifying.
Raffinate is flowed out from adsorption tower, enters raffinate column charging blending tank (V-205) through revolving valve and flowmeter.Raffinate
Liquid removes raffinate flash tank (V- through discharge control valve decompression after multiple injectors in V-205 inlet manifold are uniformly mixed
214) it is flashed, tank deck gas enters Extract tower (C-201), and tank deck liquid is by going the light wax of raffinate-to steam again after pump pressurization
Enter raffinate column (C-201) after column overhead heat exchanger (E-224) heat exchange and carries out rectifying.
Pipeline purging liquid is the mixture of n-alkane, desorbing agent.To avoid material in extract pipeline from returning to suction
Attached tower and cause a part of n-alkane to be lost in raffinate, therefore by this partial material first before desorbing agent inlet
A pipeline excludes.The pumping come out after flowmeter and control valve decompression with V-206 from the pipeline purging liquid that revolving valve flows out
Liquid is mixed into flash tank out.
Feed liquid between adsorption tower R-201AB is recycled by circulating pump (P-205AB), and circulating pump is from adsorption tower R-
The bottom 201B extracts feed liquid out, enters at the top of R-201A after pressurization through flowmeter, when the pump is in adsorption tower each region in succession
When, circular flow is by revolving valve program setting flowmeter frequency converter chain control.Circulating-pump outlet is equipped with in-line meter dielectric
Constant recorder is formed with the feed liquid for checking each region.It is equipped with ball valve valve on each bed pipeline of adsorption tower, works as lattice
Sieve on grid has leaked or has encountered other situations, can cut off the bed to break down, and the lower end of each bed is equipped with blind plate
Short tube is for unloading molecular sieve.
Desorbing agent in raffinate column is distillated from tower top, successively through raffinate column head space cooler (AC-201), raffinate column
Enter raffinate column return tank (V-201) after pushing up cooler (E-206) condensation cooling.Raffinate column reflux pump (P-201AB) is certainly
Extract desorbing agent in return tank out, outlet is divided into four tunnels, returns C-201 tower top all the way as top reflux, returns C-203 tower top all the way
Reflux, in addition removes desorbing agent compensator (V-204) by tank liquid level and flow serials control regulating valve all the way, finally goes to take off all the way
Attached dose of drying system just enables when needing.
The top raffinate column C-201 tower tray is extracted one side line material out and is increased by raffinate column side line delivery pump (P-212AB)
It goes after exchanging heat to feed to desorbing agent fractionating column C-203 after pressure.Tower reactor discharging after raffinate column bottoms pump (P-206AB) pressurization by entering
Isoparaffin knockout tower and stripper.
Through detecting, 61 DEG C of flash-point > of the liquid hydrocarbon composition containing isoparaffin component that stripper tower bottom obtains,
Not comprising cycloalkane, 195-210 DEG C of boiling range, 86 DEG C of aniline point, arene content < 50ppm, KB value 27, colorless and transparent, free from extraneous odour.
Wherein, the isoparaffin accounting that carbon number is 10 is 6%, and the isoparaffin accounting that carbon number is 11 is 35%, the isomery that carbon number is 12
Alkane accounting is 55%.The main chain carbon number of isoparaffin is 6-16, and branch carbon number is 1-6.75% branch is located at No. 2 carbon, and 20%
Branch is located at No. 3 carbon.Methyl accounting 82% in branch.The isoparaffin that carbon number is 10 is 2- methylnonane.Isoparaffin content
> 99%.
Comparative example 1
Using the technique and raw material of embodiment, it does not include isomeric alkane that difference, which is only with an isoparaffin knockout tower,
Hydrocarbon side stripper.Obtained product is very single, is unable to satisfy meticulous market demand.Isoparaffin side stripper is replaced
It is changed to plate separation tower, then can energy consumption be increased.From from the 5th, 9,15 layer three of isoparaffin knockout tower side line tower tray middle and upper part
Extract stream enters isoparaffin side stripper, obtains 61 DEG C of flash-point > of the liquid hydrocarbon combination containing isoparaffin component
Low energy consumption for object, and yield is big, and the product market demand is big.
Comparative example 2
Using the technique of embodiment, the ratio of n-alkane in raw material and isoparaffin is controlled as C5-C9 n-alkane:
Isoparaffin=8 C5-C9: 1, C10-C13 n-alkane: isoparaffin=2 C10-C13: 1, C14-C16 n-alkane: C14-
Isoparaffin=2.2 C16: 1, C17+ n-alkane: isoparaffin=2.1 C17+: 1.Then point of n-alkane and isoparaffin
From inefficient, the molecular sieve service life is short, and isoparaffin purity is only 90% in product.
Comparative example 3
Using the technique and raw material of embodiment, difference is the cycloalkane in raw material comprising 2wt%.Obtained liquid hydrocarbon
The flash-point of composition product is only 57 DEG C, isoparaffin product purity 85%.The product belongs to dangerous material, and transport is inconvenient, market
Demand is small, and economic value is lower.
Claims (6)
1. a kind of liquid hydrocarbon composition containing isoparaffin component, it is characterised in that: liquid hydrocarbon composition is passed through by raw material
Cross pretreatment, adsorbing separation, fractionation process are prepared；Fractionation process first takes out the isoparaffin from adsorptive separation technology
Extraction raffinate is passed through isoparaffin knockout tower, and normal paraffin content is lower than 2% in isoparaffin raffinate, from isoparaffin knockout tower side
Transmission tower disk extract stream enters isoparaffin side stripper, and stripper tower bottom obtains 61 DEG C of flash-point > and contains isoparaffin group
The liquid hydrocarbon composition divided；Isoparaffin side stripper stripped overhead steam returns to isoparaffin knockout tower；Isoparaffin
The tower top pressure 0.08-0.11MPa of knockout tower, tower bottom pressure 0.12-0.15MPa, 198-210 DEG C of tower top temperature, column bottom temperature
270-290℃；The tower top pressure 0.09-0.12MPa of isoparaffin side stripper, tower bottom pressure 0.10-0.13MPa, tower top
200-220 DEG C of temperature, 205-225 DEG C of column bottom temperature；In raw material, C5-C9 n-alkane: C5-C9 isoparaffin=(2-5): 1,
C10-C13 n-alkane: C10-C13 isoparaffin=(0.8-1): 1, C14-C16 n-alkane: C14-C16 isoparaffin=
(1-1.2): 1, C17+ n-alkane: C17+ isoparaffin=(1-1.2): 1.
2. the liquid hydrocarbon composition according to claim 1 containing isoparaffin component, it is characterised in that: raw material is free of
Cycloalkane.
3. the liquid hydrocarbon composition according to claim 1 containing isoparaffin component, it is characterised in that: enter isomery
The stream of alkane side stripper is by the extraction of the 5th, 9,15 layer three of isoparaffin knockout tower side line tower tray middle and upper part.
4. the liquid hydrocarbon composition according to claim 1 containing isoparaffin component, it is characterised in that: adsorbing separation
For molecular sieve adsorbing separation, 176-180 DEG C of technological temperature, pressure 2.2-2.5MPa.
5. the liquid hydrocarbon composition according to claim 1 containing isoparaffin component, it is characterised in that: pre-process and be
De- light, the de- weight of weight-removing column of lightness-removing column, the tower top pressure 0.01-0.05MPa of lightness-removing column, tower bottom pressure 0.02-0.06MPa, tower top
155-165 DEG C of temperature, 210-230 DEG C of column bottom temperature；The tower top pressure 9-13KPa of weight-removing column, tower bottom pressure 15-25KPa, tower top
110-130 DEG C of temperature, 220-250 DEG C of column bottom temperature.
6. the liquid hydrocarbon composition according to claim 4 containing isoparaffin component, it is characterised in that: molecular sieve is empty
The ratio of n-alkane volume is 1.15-1.55 in cave volume and raw material.
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| CN111471484A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | Process for preparing isoparaffin composition |
| CN111471488A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | High-purity environment-friendly isoparaffin solvent oil and application thereof |
| CN111471486A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | Isoparaffin solvent oil composition prepared from coal indirect liquefied product serving as raw material |
| CN111471483A (en) * | 2019-01-23 | 2020-07-31 | 内蒙古伊泰宁能精细化工有限公司 | Method for producing series of high-purity isoparaffins |
| CN111635779B (en) * | 2020-05-27 | 2022-04-12 | 华阳新兴科技（天津）集团有限公司 | Method for preparing high-quality aluminum foil rolling base oil and application |
| CN114933917B (en) * | 2022-06-28 | 2023-08-22 | 福建清油夫实业有限公司 | Method for cleaning heat conduction system without stopping production and repairing heat conduction oil on line |
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