CN106167718B - A kind of de-oiling method of the gas of hydrocarbon containing conventional gas and conventional liq hydrocarbon inferior - Google Patents
A kind of de-oiling method of the gas of hydrocarbon containing conventional gas and conventional liq hydrocarbon inferior Download PDFInfo
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- CN106167718B CN106167718B CN201610550628.8A CN201610550628A CN106167718B CN 106167718 B CN106167718 B CN 106167718B CN 201610550628 A CN201610550628 A CN 201610550628A CN 106167718 B CN106167718 B CN 106167718B
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- 238000000034 method Methods 0.000 title claims abstract description 163
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 159
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 157
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 154
- 239000007789 gas Substances 0.000 claims abstract description 98
- 230000008569 process Effects 0.000 claims abstract description 98
- 238000010521 absorption reaction Methods 0.000 claims abstract description 80
- 239000011280 coal tar Substances 0.000 claims abstract description 47
- 239000000047 product Substances 0.000 claims abstract description 43
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 39
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 25
- 230000002745 absorbent Effects 0.000 claims abstract description 20
- 239000002250 absorbent Substances 0.000 claims abstract description 20
- 238000004939 coking Methods 0.000 claims abstract description 13
- 238000004227 thermal cracking Methods 0.000 claims abstract description 13
- 239000003921 oil Substances 0.000 claims description 155
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 51
- 239000001257 hydrogen Substances 0.000 claims description 49
- 229910052739 hydrogen Inorganic materials 0.000 claims description 49
- 239000007788 liquid Substances 0.000 claims description 30
- 238000009835 boiling Methods 0.000 claims description 27
- 239000000295 fuel oil Substances 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 11
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 7
- 239000010734 process oil Substances 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 6
- 238000007233 catalytic pyrolysis Methods 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 6
- 239000003208 petroleum Substances 0.000 claims description 6
- 239000011269 tar Substances 0.000 claims description 6
- 238000004523 catalytic cracking Methods 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000003912 environmental pollution Methods 0.000 claims description 3
- 239000010763 heavy fuel oil Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 125000001477 organic nitrogen group Chemical group 0.000 claims description 3
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims description 3
- 239000003079 shale oil Substances 0.000 claims description 3
- 239000011275 tar sand Substances 0.000 claims description 3
- 238000006011 modification reaction Methods 0.000 claims 1
- 125000001741 organic sulfur group Chemical group 0.000 claims 1
- 238000005238 degreasing Methods 0.000 abstract description 5
- 238000004821 distillation Methods 0.000 abstract description 4
- 238000000746 purification Methods 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- 238000011084 recovery Methods 0.000 abstract description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
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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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A kind of de-oiling method of the gas of hydrocarbon containing conventional gas and conventional liq hydrocarbon inferior, hot procedure P01 particularly suitable for coal tar such as heats distillation, coking, thermal cracking, the hydro-upgrading process HU's for the oil product APY that the gas APG of hydrocarbon containing conventional gas caused by either shallow hydrogenation process etc. and conventional liq hydrocarbon inferior degreasing process AP and AP is obtained is applied in combination, separation hydro-upgrading process HU hydrogenation reaction product HUP obtains the HUPY of logistics containing hydrocarbon ils, it is to absorb the conventional liq hydrocarbon inferior in oily AS absorption gases APG to obtain rich absorbent oil RS using at least a portion HUPY and/or at least a portion APY, rich absorbent oil uses as oil product APY hydro-upgrading process HU raw material, the gas APG de-oiling purification and the recovery upgrading of hydrocarbon inferior with flow simple realization.
Description
Technical field
The present invention relates to a kind of hydrocarbon containing conventional gas and the de-oiling method of the gas of conventional liq hydrocarbon inferior, particularly suitable for
The hot procedure PU of coal tar as caused by heating distillation, coking, thermal cracking, either shallow hydrogenation process etc. hydrocarbon containing conventional gas and
The hydro-upgrading process HU for the oil product APY that the gas PUG of conventional liq hydrocarbon inferior degreasing process AP and AP is obtained combination makes
With, separation hydro-upgrading process HU hydrogenation reaction product HUP obtains the HUPY of logistics containing hydrocarbon ils, using at least a portion HUPY with
Or at least a portion APY is to absorb the conventional liq hydrocarbon inferior that oily AS is absorbed in gas PUG to obtain rich absorbent oil RS, rich absorbent oil
Raw material as oil product APY hydro-upgrading process HU uses, the gas PUG de-oiling purification and inferior with flow simple realization
The recovery upgrading of hydrocarbon.
Background technology
The hot procedure PU of coal tar of the present invention, can be that heating distillation, coking, thermal cracking, either shallow were hydrogenated with
The processes such as journey, it is the gas PUG for producing hydrocarbon containing conventional gas and conventional liq hydrocarbon inferior the characteristics of hot procedure PU.
At present, it there is no the hot procedure PU of the coal tar hydrocarbon containing conventional gas as caused by heating the vacuum tower of still-process
With conventional liq hydrocarbon SD inferior (sulfur-bearing, nitrogenous, containing aromatic hydrocarbons) gas PUG degreasing process AP Perfected process report, if
These gases go heating furnace burning to cause black smoke pollution environment because of imperfect combustion, if absorbing gas with clean oil product
Conventional liq hydrocarbon SD inferior then causes to absorb oil and be contaminated to be difficult to regenerate in PUG, if absorbed with other hydrocarbon inferior in gas PUG
Conventional liq hydrocarbon SD inferior can not then ensure the de-oiling effect of gas.
On the other hand, the hydro-upgrading process HU for the oil product APY that the hot procedure PU of coal tar is obtained, it usually needs make
By the use of hydrogenated oil or its distillate as flux oil of the recycle oil as oil product APY or circulation hydrogenated oil (such as in order to be hydrogenated with
Cracking or deep hydrofinishing), these circulation hydrocarbon ils, which are actually that gas PUG degreasing process AP ideal is free, to be absorbed
Oil, that is, form the secondary of recycle oil and be used in series.
The de-oiling method of the gas of a kind of hydrocarbon containing conventional gas of the invention and conventional liq hydrocarbon inferior, particularly suitable for coal tar
The hot procedure PU of oil hydrocarbon containing conventional gas and poor quality as caused by heating distillation, coking, thermal cracking, either shallow hydrogenation process etc.
The hydro-upgrading process HU's for the oil product APY that the gas PUG of conventional liq hydrocarbon degreasing process AP and AP is obtained is applied in combination, its
Basic conception is：Separation hydro-upgrading process HU hydrogenation reaction product HUP obtains the HUPY of logistics containing hydrocarbon ils, utilizes at least one
It is to absorb the conventional liq hydrocarbon inferior that oily AS is absorbed in gas PUG to obtain rich absorbent oil RS to divide HUPY, and rich absorbent oil is as oil product
APY hydro-upgrading process HU raw material uses, the gas PUG de-oiling purification and the recovery of hydrocarbon inferior with flow simple realization
Upgrading.Absorption process, it is possible to use at least a portion APY is the first absorption oil, using the HUPY of logistics containing hydrocarbon ils to reabsorb oil.
The inventive method has no report.
The purpose of invention is the de-oiling method for proposing the gas of a kind of hydrocarbon containing conventional gas and conventional liq hydrocarbon inferior.
The content of the invention
The de-oiling method of the gas of a kind of hydrocarbon containing conventional gas of the invention and conventional liq hydrocarbon inferior, it is characterised in that：
1. in low hydrogen content hydrocarbon HDS hot procedure PU, hydrocarbon containing conventional gas and conventional liq hydrocarbon SD inferior are obtained
Gas PUG and oil product APY；
Low hydrogen content hydrocarbon HDS hot procedure PU, selected from heating still-process or coking or thermal cracking process or
Either shallow hydrogenation process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process；
The conventional liq hydrocarbon SD inferior, refer to that directly burning causes the hydro carbons of environmental pollution, containing having at least partially
Machine sulphur or at least a portion organic nitrogen or at least a portion aromatic hydrocarbons；
At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；
2. in hydro-upgrading process HU, under hydrogen and hydrogenation catalyst HUC existence conditions, Hydrogenation raw oil HU-F1 is complete
Hydro-upgrading reaction product HUP is converted into hydro-upgrading reaction HUR；
Separation hydro-upgrading reaction product HUP obtains logistics containing hydrocarbon ils HUPY, logistics HUPY and enters the step 3. absorption
Process ASU is used as absorbing oily AS；
3. it is changed into de-oiling gas with absorbing oily AS and completing to separate at least once in absorption process ASU, gas PUG
PUG-DO and rich absorbent oil RS, rich absorbent oil RS contact into hydro-upgrading process HU with hydrogenation catalyst HUC to carry out hydrogenation and changes
Qualitative response.
Low hydrogen content hydrocarbon HDS, the one or more being generally selected from following materials：
1. oil product obtained by coalite tar or its distillate or its hot procedure；The hot procedure PU, for heating
Still-process or coking or thermal cracking process or either shallow hydrogenation process；
2. oil product obtained by medium temperature coal tar or its distillate or its hot procedure；
3. oil product obtained by high temperature coal-tar or its distillate or its hot procedure；
4. oil product obtained by liquefied coal coil or its distillate obtained by coal liquefaction or its hot procedure；
5. oil product obtained by shale oil or its distillate or its hot procedure；
6. oil product obtained by tar sand base heavy oil or its hot procedure；
7. petroleum base wax oil thermal cracking tars；
8. oil product obtained by petroleum based heavy fuel oils hot procedure, hot procedure is coking heavy oil process or RFCC
Process or heavy oil catalytic pyrolysis process；
9. other polycyclic aromatic hydrocarbon concentration are higher than 40% hydrocarbon ils higher than 10%, aromatic hydrocarbons total content.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, operating condition is usually：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. hydro-upgrading process HU operating condition is：Temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen
Gas/feedstock oil volume ratio is 50~5000；
The oily AS of absorption that separation hydro-upgrading reaction product HUP is obtained is mainly by hydrocarbon group that normal boiling point is 80~350 DEG C
It is grouped into；
3. in absorption process ASU, gas PUG completes 2~20 contact separations with absorbing oily AS.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, operating condition is generally：
1. low hydrogen content hydrocarbon HDS is coal tar；
Formed 2. absorbing oily AS and being mainly 80~350 DEG C by normal boiling point；
3. in absorption process ASU, tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is
45~65 DEG C；It is K100, K100 0.5 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG,
~20.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, operating condition is preferably：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. absorb oily AS to be mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C；
3. in absorption process ASU, tower top pressure is 0.6~1.40MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is
45~65 DEG C；It is K100, K100 1.0 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG,
~4.0.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is usually using operating condition during biabsorption oil：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. absorption oil AS1 and reabsorb oily AS2 that separation hydro-upgrading reaction product HUP is obtained；
AS1 is mainly made up of the hydrocarbon component that normal boiling point is 80~220 DEG C；
AS2 is mainly made up of the hydrocarbon component that normal boiling point is 220~350 DEG C；
3. contacted in absorption process ASU, gas PUG with absorbing after oily AS1 is contacted with reabsorbing oily AS2；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
The ratio that definition absorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K100, K100 for 0.5~
20；
It is K200 that definition, which reabsorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K200 is
0.01~2.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is generally using operating condition during biabsorption oil：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. absorption oil AS1 and reabsorb oily AS2 that separation hydro-upgrading reaction product HUP is obtained；
AS1 is mainly made up of the hydrocarbon component that normal boiling point is 80~220 DEG C；
AS2 is mainly made up of the hydrocarbon component that normal boiling point is 220~350 DEG C；
3. contacted in absorption process ASU, gas PUG with absorbing after oily AS1 is contacted with reabsorbing oily AS2；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
The ratio that definition absorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K100, K100 for 1.0~
4.0；
It is K200 that definition, which reabsorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K200 is
0.05~1.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is usually using operating condition when pre-absorption is oily, absorption is oily：
1. low hydrogen content hydrocarbon HDS is coal tar；
At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；
At least a portion Hydrogenation raw oil HU-F1 enters the step 3. absorption process ASU as pre-absorption oil BAS；
2. the absorption oil AS that separation hydro-upgrading reaction product HUP is obtained；
AS is mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C；
3. in absorption process ASU, gas PUG contacted with pre-absorption oil BAS after with absorb oily AS separate be changed into it is de-
Oil gas body PUG-DO and rich absorbent oil RS；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
The ratio for defining pre-absorption oil BAS molecular numbers and the molecular number of conventional liquid hydrocarbon in gas PUG is KB, KB 0.05
~20；
It is K100, K100 0.01 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG,
~20.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is generally using operating condition when pre-absorption is oily, absorption is oily：
1. low hydrogen content hydrocarbon HDS is coal tar；
At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；
At least a portion Hydrogenation raw oil HU-F1 enters the step 3. absorption process ASU as pre-absorption oil BAS；
2. the absorption oil AS that separation hydro-upgrading reaction product HUP is obtained；
AS is mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C.
3. in absorption process ASU, gas PUG contacted with pre-absorption oil BAS after with absorb oily AS separate be changed into it is de-
Oil gas body PUG-DO and rich absorbent oil RS；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
KB is 1.0~4；
The ratio that definition absorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K100, K100 for 1.0~
4。
The present invention, operation target are usually：
3. at least 70% of conventional liquid hydrocarbon in absorption process ASU, gas PUG is absorbed.
Embodiment
The de-oiling method of the gas of a kind of hydrocarbon containing conventional gas of the invention and conventional liq hydrocarbon inferior, it is characterised in that：
1. in low hydrogen content hydrocarbon HDS hot procedure PU, hydrocarbon containing conventional gas and conventional liq hydrocarbon SD inferior are obtained
Gas PUG and oil product APY；
Low hydrogen content hydrocarbon HDS hot procedure PU, selected from heating still-process or coking or thermal cracking process or
Either shallow hydrogenation process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process；
The conventional liq hydrocarbon SD inferior, refer to that directly burning causes the hydro carbons of environmental pollution, containing having at least partially
Machine sulphur or at least a portion organic nitrogen or at least a portion aromatic hydrocarbons；
At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；
2. in hydro-upgrading process HU, under hydrogen and hydrogenation catalyst HUC existence conditions, Hydrogenation raw oil HU-F1 is complete
Hydro-upgrading reaction product HUP is converted into hydro-upgrading reaction HUR；
Separation hydro-upgrading reaction product HUP obtains logistics containing hydrocarbon ils HUPY, logistics HUPY and enters the step 3. absorption
Process ASU is used as absorbing oily AS；
3. it is changed into de-oiling gas with absorbing oily AS and completing to separate at least once in absorption process ASU, gas PUG
PUG-D0 and rich absorbent oil RS, rich absorbent oil RS contact into hydro-upgrading process HU with hydrogenation catalyst HUC to carry out hydrogenation and changes
Qualitative response.
Low hydrogen content hydrocarbon HDS, the one or more being generally selected from following materials：
1. oil product obtained by coalite tar or its distillate or its hot procedure；The hot procedure PU, for heating
Still-process or coking or thermal cracking process or either shallow hydrogenation process；
2. oil product obtained by medium temperature coal tar or its distillate or its hot procedure；
3. oil product obtained by high temperature coal-tar or its distillate or its hot procedure；
4. oil product obtained by liquefied coal coil or its distillate obtained by coal liquefaction or its hot procedure；
5. oil product obtained by shale oil or its distillate or its hot procedure；
6. oil product obtained by tar sand base heavy oil or its hot procedure；
7. petroleum base wax oil thermal cracking tars；
8. oil product obtained by petroleum based heavy fuel oils hot procedure, hot procedure is coking heavy oil process or RFCC
Process or heavy oil catalytic pyrolysis process；
9. other polycyclic aromatic hydrocarbon concentration are higher than 40% hydrocarbon ils higher than 10%, aromatic hydrocarbons total content.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, operating condition is usually：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. hydro-upgrading process HU operating condition is：Temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen
Gas/feedstock oil volume ratio is 50~5000；
The oily AS of absorption that separation hydro-upgrading reaction product HUP is obtained is mainly by hydrocarbon group that normal boiling point is 80~350 DEG C
It is grouped into；
3. in absorption process ASU, gas PUG completes 2~20 contact separations with absorbing oily AS.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, operating condition is generally：
1. low hydrogen content hydrocarbon HDS is coal tar；
Formed 2. absorbing oily AS and being mainly 80~350 DEG C by normal boiling point；
3. in absorption process ASU, tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is
45~65 DEG C；It is K100, K100 0.5 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG,
~20.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, operating condition is preferably：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. absorb oily AS to be mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C；
3. in absorption process ASU, tower top pressure is 0.6~1.40MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is
45~65 DEG C；It is K100, K100 1.0 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG,
~4.0.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is usually using operating condition during biabsorption oil：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. absorption oil AS1 and reabsorb oily AS2 that separation hydro-upgrading reaction product HUP is obtained；
AS1 is mainly made up of the hydrocarbon component that normal boiling point is 80~220 DEG C；
AS2 is mainly made up of the hydrocarbon component that normal boiling point is 220~350 DEG C；
3. contacted in absorption process ASU, gas PUG with absorbing after oily AS1 is contacted with reabsorbing oily AS2；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
The ratio that definition absorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K100, K100 for 0.5~
20；
It is K200 that definition, which reabsorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K200 is
0.01~2.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is generally using operating condition during biabsorption oil：
1. low hydrogen content hydrocarbon HDS is coal tar；
2. absorption oil AS1 and reabsorb oily AS2 that separation hydro-upgrading reaction product HUP is obtained；
AS1 is mainly made up of the hydrocarbon component that normal boiling point is 80~220 DEG C；
AS2 is mainly made up of the hydrocarbon component that normal boiling point is 220~350 DEG C；
3. contacted in absorption process ASU, gas PUG with absorbing after oily AS1 is contacted with reabsorbing oily AS2；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
The ratio that definition absorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K100, K100 for 1.0~
4.0；
It is K200 that definition, which reabsorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K200 is
0.05~1.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is usually using operating condition when pre-absorption is oily, absorption is oily：
1. low hydrogen content hydrocarbon HDS is coal tar；
At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；
At least a portion Hydrogenation raw oil HU-F1 enters the step 3. absorption process ASU as pre-absorption oil BAS；
2. the absorption oil AS that separation hydro-upgrading reaction product HUP is obtained；
AS is mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C；
3. in absorption process ASU, gas PUG contacted with pre-absorption oil BAS after with absorb oily AS separate be changed into it is de-
Oil gas body PUG-DO and rich absorbent oil RS；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
The ratio for defining pre-absorption oil BAS molecular numbers and the molecular number of conventional liquid hydrocarbon in gas PUG is KB, KB 0.05
~20；
It is K100, K100 0.01 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG,
~20.
The present invention, when low hydrogen content hydrocarbon HDS is coal tar, it is generally using operating condition when pre-absorption is oily, absorption is oily：
1. low hydrogen content hydrocarbon HDS is coal tar；
At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；
At least a portion Hydrogenation raw oil HU-F1 enters the step 3. absorption process ASU as pre-absorption oil BAS；
2. the absorption oil AS that separation hydro-upgrading reaction product HUP is obtained；
AS is mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C.
3. in absorption process ASU, gas PUG contacted with pre-absorption oil BAS after with absorb oily AS separate be changed into it is de-
Oil gas body PUG-DO and rich absorbent oil RS；
Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；
KB is 1.0~4；
The ratio that definition absorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K100, K100 for 1.0~
4。
The present invention, operation target are usually：
3. at least 70% of conventional liquid hydrocarbon in absorption process ASU, gas PUG is absorbed.
The advantage of the invention is that：
1. absorbing oil borrows hydro-upgrading process HU recycle oils, it is not necessary to special absorptive oil；
2. the regenerative system of the absorber component in rich absorbent oil, borrow hydro-upgrading process HU and hydro-upgrading reaction production
Thing HUP is separated or fractionating system is completed；
The processing that cleans of conventional liq hydrocarbon SD inferior in rich absorbent oil is reclaimed, and the hydrogenation for borrowing processing oil product APY changes
Matter process HU and hydro-upgrading reaction product HUP separation or fractionating system are completed；
3. the present invention is suitable for new device or existing apparatus transformation.
Gas PUG enters before absorption process ASU processes, it may be necessary to which compressor pressurizes.
Claims (10)
- A kind of 1. de-oiling method of the gas of hydrocarbon containing conventional gas and conventional liq hydrocarbon inferior, it is characterised in that：1. in low hydrogen content hydrocarbon HDS hot procedure PU, hydrocarbon containing conventional gas and conventional liq hydrocarbon SD inferior gas are obtained PUG and oil product APY；Low hydrogen content hydrocarbon HDS hot procedure PU, selected from heating still-process or coking or thermal cracking process or either shallow Hydrogenation process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process；The conventional liq hydrocarbon SD inferior, refer to that directly burning causes the hydro carbons of environmental pollution, organic sulfur containing at least a portion Or at least a portion organic nitrogen or at least a portion aromatic hydrocarbons；At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；2. in hydro-upgrading process HU, under hydrogen and hydrogenation catalyst HUC existence conditions, Hydrogenation raw oil HU-F1 completes to add Hydrogen modification reaction HUR is converted into hydro-upgrading reaction product HUP；Separation hydro-upgrading reaction product HUP obtains logistics containing hydrocarbon ils HUPY, logistics HUPY and enters the step 3. absorption process ASU is used as absorbing oily AS；3. it is changed into de-oiling gas PUG-DO with absorbing oily AS and completing to separate at least once in absorption process ASU, gas PUG Contacted into hydro-upgrading process HU with hydrogenation catalyst HUC with rich absorbent oil RS, rich absorbent oil RS and carry out hydro-upgrading reaction.
- 2. method according to claim 1, it is characterised in that：Low hydrogen content hydrocarbon HDS, the one or more in following materials：1. oil product obtained by coalite tar or its distillate or its hot procedure；The hot procedure PU, distilled for heating Process or coking or thermal cracking process or either shallow hydrogenation process；2. oil product obtained by medium temperature coal tar or its distillate or its hot procedure；3. oil product obtained by high temperature coal-tar or its distillate or its hot procedure；4. oil product obtained by liquefied coal coil or its distillate obtained by coal liquefaction or its hot procedure；5. oil product obtained by shale oil or its distillate or its hot procedure；6. oil product obtained by tar sand base heavy oil or its hot procedure；7. petroleum base wax oil thermal cracking tars；8. oil product obtained by petroleum based heavy fuel oils hot procedure, hot procedure is coking heavy oil process or heavy oil catalytic cracking process Or heavy oil catalytic pyrolysis process；9. other polycyclic aromatic hydrocarbon concentration are higher than 40% hydrocarbon ils higher than 10%, aromatic hydrocarbons total content.
- 3. method according to claim 1, it is characterised in that：1. low hydrogen content hydrocarbon HDS is coal tar；2. hydro-upgrading process HU operating condition is：Temperature is 170~460 DEG C, pressure is 4.0~28.0MPa, hydrogen/original It is 50~5000 to expect oil volume ratio；The oily AS of absorption that separation hydro-upgrading reaction product HUP is obtained is mainly by hydrocarbon component group that normal boiling point is 80~350 DEG C Into；3. in absorption process ASU, gas PUG completes 2~20 contact separations with absorbing oily AS.
- 4. method according to claim 1, it is characterised in that：1. low hydrogen content hydrocarbon HDS is coal tar；Formed 2. absorbing oily AS and being mainly 80~350 DEG C by normal boiling point；3. in absorption process ASU, tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, column bottom temperature be 45~ 65℃；It is K100 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K100 is 0.5~20.
- 5. method according to claim 1, it is characterised in that：1. low hydrogen content hydrocarbon HDS is coal tar；2. absorb oily AS to be mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C；3. in absorption process ASU, tower top pressure is 0.6~1.40MPa, tower top temperature is 40~60 DEG C, column bottom temperature be 45~ 65℃；The ratio that definition absorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K100, K100 for 1.0~ 4.0。
- 6. method according to claim 1, it is characterised in that：1. low hydrogen content hydrocarbon HDS is coal tar；2. absorption oil AS1 and reabsorb oily AS2 that separation hydro-upgrading reaction product HUP is obtained；AS1 is mainly made up of the hydrocarbon component that normal boiling point is 80~220 DEG C；AS2 is mainly made up of the hydrocarbon component that normal boiling point is 220~350 DEG C；3. contacted in absorption process ASU, gas PUG with absorbing after oily AS1 is contacted with reabsorbing oily AS2；Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；It is K100 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K100 is 0.5~20；The ratio that definition reabsorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K200, K200 for 0.01~ 2。
- 7. method according to claim 1, it is characterised in that：1. low hydrogen content hydrocarbon HDS is coal tar；2. absorption oil AS1 and reabsorb oily AS2 that separation hydro-upgrading reaction product HUP is obtained；AS1 is mainly made up of the hydrocarbon component that normal boiling point is 80~220 DEG C；AS2 is mainly made up of the hydrocarbon component that normal boiling point is 220~350 DEG C；3. contacted in absorption process ASU, gas PUG with absorbing after oily AS1 is contacted with reabsorbing oily AS2；Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；It is K100 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K100 is 1.0~4.0；The ratio that definition reabsorbs the molecular number of conventional liquid hydrocarbon in oil subnumber and gas PUG be K200, K200 for 0.05~ 1。
- 8. method according to claim 1, it is characterised in that：1. low hydrogen content hydrocarbon HDS is coal tar；At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；At least a portion Hydrogenation raw oil HU-F1 enters the step 3. absorption process ASU as pre-absorption oil BAS；2. the absorption oil AS that separation hydro-upgrading reaction product HUP is obtained；AS is mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C；3. in absorption process ASU, gas PUG is separate after being contacted with pre-absorption oil BAS with the oily AS of absorption is changed into de-oiling gas Body PUG-DO and rich absorbent oil RS；Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；The ratio for defining the molecular number of conventional liquid hydrocarbon in pre-absorption oil BAS molecular numbers and gas PUG be KB, KB for 0.05~ 20；It is K100 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K100 is 0.01~20.
- 9. method according to claim 1, it is characterised in that：1. low hydrogen content hydrocarbon HDS is coal tar；At least a portion oil product APY enters step, and 2. the hydro-upgrading process HU is used as Hydrogenation raw oil HU-F1；At least a portion Hydrogenation raw oil HU-F1 enters the step 3. absorption process ASU as pre-absorption oil BAS；2. the absorption oil AS that separation hydro-upgrading reaction product HUP is obtained；AS is mainly made up of the hydrocarbon component that normal boiling point is 80~350 DEG C；3. in absorption process ASU, gas PUG is separate after being contacted with pre-absorption oil BAS with the oily AS of absorption is changed into de-oiling gas Body PUG-DO and rich absorbent oil RS；Tower top pressure is 0.4~1.80MPa, tower top temperature is 40~60 DEG C, and column bottom temperature is 45~65 DEG C；KB is 1.0~4；It is K100 that definition, which absorbs oil subnumber and the ratio of the molecular number of conventional liquid hydrocarbon in gas PUG, and K100 is 1.0~4.
- 10. method according to claim 1, it is characterised in that：3. at least 70% of conventional liquid hydrocarbon in absorption process ASU, gas PUG is absorbed.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101126034A (en) * | 2006-08-18 | 2008-02-20 | 张海龙 | Method for producing diesel oil by coal tar cracking and hydrogenation |
| CN101712889A (en) * | 2009-11-26 | 2010-05-26 | 湖南长岭石化科技开发有限公司 | Method for preparing light aromatics from coal tar |
| CN102041084A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Heavy hydrocarbon hydrogenation combined process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101126034A (en) * | 2006-08-18 | 2008-02-20 | 张海龙 | Method for producing diesel oil by coal tar cracking and hydrogenation |
| CN102041084A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Heavy hydrocarbon hydrogenation combined process |
| CN101712889A (en) * | 2009-11-26 | 2010-05-26 | 湖南长岭石化科技开发有限公司 | Method for preparing light aromatics from coal tar |
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