CN106047406A - Coal tar hydrogenation reaction device and method for rapidly recycling light hydrocarbons - Google Patents
Coal tar hydrogenation reaction device and method for rapidly recycling light hydrocarbons Download PDFInfo
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- CN106047406A CN106047406A CN201610552334.9A CN201610552334A CN106047406A CN 106047406 A CN106047406 A CN 106047406A CN 201610552334 A CN201610552334 A CN 201610552334A CN 106047406 A CN106047406 A CN 106047406A
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- Prior art keywords
- outer tube
- section
- lighter hydrocarbons
- cone
- leading portion
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Links
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 81
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 81
- 239000011280 coal tar Substances 0.000 title claims abstract description 38
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000004064 recycling Methods 0.000 title abstract 5
- 239000007789 gas Substances 0.000 claims abstract description 49
- 238000011084 recovery Methods 0.000 claims abstract description 46
- 238000006243 chemical reaction Methods 0.000 claims abstract description 28
- 239000001257 hydrogen Substances 0.000 claims abstract description 25
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 25
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 10
- 238000004517 catalytic hydrocracking Methods 0.000 claims description 7
- 238000007373 indentation Methods 0.000 claims description 6
- 230000004323 axial length Effects 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 4
- 238000009827 uniform distribution Methods 0.000 claims description 3
- 238000005336 cracking Methods 0.000 abstract description 4
- 238000000197 pyrolysis Methods 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 21
- 239000003795 chemical substances by application Substances 0.000 description 9
- 239000003245 coal Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000011269 tar Substances 0.000 description 4
- 238000004939 coking Methods 0.000 description 3
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 239000011287 low-temperature tar Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 239000008161 low-grade oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003223 protective agent Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001502 supplementing effect 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
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
-
- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
-
- 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
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
Landscapes
- Chemical & Material Sciences (AREA)
- 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
The invention relates to a coal tar hydrogenation reaction device and method for rapidly recycling light hydrocarbons. The device comprises a light hydrocarbon recycling section and a hydrogenation reaction section; the light hydrocarbon recycling section comprises an outer tube, a middle cone and a pressure recovery segment, the outer tube comprises a front end portion and a rear end portion, the middle cone is completely located in the outer tube and comprises a cone bottom, a cone body and an extension tube which are sequentially connected, 6-10 guide vanes are evenly distributed in the radial direction of the cone body, the included angle between each guide vane and the axial direction of the middle cone ranges from 30 degrees to 60 degrees, and the pressure recovery segment is connected with the rear end of the extension tube and the rear end of the outer tube; the hydrogenation reaction section comprises a raw oil inlet, a hydrogen inlet, a product oil outlet and a gas outlet which is coupled with the front end of the outer tube. According to the coal tar hydrogenation reaction device and method for rapidly recycling the light hydrocarbons, the temperature and pressure of pyrolysis gas generated through a coal tar hydrogenation cracking reaction can be utilized, the light hydrocarbons in the pyrolysis gas are recycled at a device outlet, energy does not need to be additionally supplemented, operation is easy and convenient, and the recovery efficiency of the light hydrocarbons is high.
Description
Technical field
The present invention relates to low grade oils processing technique field, the coal tar hydrogenating particularly relating to a kind of quick recovery lighter hydrocarbons is anti-
Answer device and method.
Background technology
Along with developing rapidly of modern industry, within considerably long period, China will be day by day to the demand of fossil energy
Increase.And the energy general layout of China's " rich coal, gas oil-poor, few ", determine coal leading position in energy strategy, coal
Clean and effective utilizes direct relation the sustainable development of national economy.Currently, China's oil external dependence degree the nearlyest 60% is logical
Crossing coal production cleaning fuel is the effective way reducing dependence on foreign countries for oil.Coking and coal sub-prime classified utilization at coal
During can produce more coal tar, to its carry out deep processing be produce cleaning fuel a kind of important way.
According to the difference of dry distillation of coal temperature, coal tar can be divided into low temperature tar (450～650 DEG C), middle low temperature tar (600
～800 DEG C), middle temperature tar (700～900 DEG C) and high temperature tar (900～1000 DEG C).Coal tar and conventional oil have bigger
Difference, along with the rising for the treatment of temperature, aromatic hydrocarbons, colloid, asphalitine and hetero atom (sulfur, nitrogen, oxygen, metal) in coal tar contain
Amount increases.A coal tar seldom part, by deep processing and utilization, is directly burnt mostly as fuel, not only causes environment dirty
Dye and be a kind of wasting of resources greatly.Along with the increase of the most harsh of environmental regulation He vehicle fuel demand, pass through
Hydrogen addition technology utilizes coal tar to produce light Fuel and is increasingly subject to the concern of people.
For the problem of above-mentioned existence, prior art one proposes the side of a kind of producing fuel oil by coal tar hydrogenation modifying
Method, after complete for pretreatment fraction coal tar and flux oil being mixed in proportion, sequentially passes through equipped with hydrogenation protecting agent, pre-hydrogenation catalyst
The either shallow hydrogenation unit of agent and the deep hydrogenation unit equipped with main hydrogenating catalyst, finally obtain light-end products.Used by the method
Flux oil derives from oil full distillate oil, reducing of crude oil distillate or coal tar hydrogenating and generates oil etc., and anti-coking effect is limited,
In coal tar, heavy component conversion ratio is low.And the introducing of flux oil had both added cost of material, reduced again tar processing amount,
Thus affect the treatment effeciency of tar.
Prior art two proposes a kind of method that heavy, residual oil is cracked into light-end products through floating bed hydrogenation.The method is selected
Floating bed hydrogenation reactor is looped back as hydrogen supply agent with the diesel oil distillate (170～350 DEG C) after hydrotreating.The method with add
The method entering diluent is similar to, and hydrogenated diesel oil circulating load is relatively big, and reduces the treatment effeciency of device in processing procedure.
Prior art three is selected naphthane or decahydronaphthalene as hydrogen supply agent, mix by a certain percentage with coal tar and add
Hydrogen reacts, and wherein hydrogen supply agent need to participate in reaction in supercriticality or under supercriticality, reduces coking rate.In reaction
Adding water in system, under high temperature, condition of high voltage, water can produce hydrogen with the coke gasification reaction generated, thus recovers the hydrogen supply of hydrogen supply agent
Ability.The method need add hydrogen supply agent, and hydrogen supply agent hydrogen supply capacity recovery extent it cannot be guaranteed that, need to constantly add fresh confession
Hydrogen agent, and hydrogen supply agent price is of a relatively high, causes processing cost higher.
Summary of the invention
The problem existed in view of prior art, it is contemplated that realize coal tar is carried out hydrotreating, and quickly reclaims
The lighter hydrocarbons product that hydrogenation reaction generates.The present invention can complete under conditions of not supplementing energy in device the recovery of lighter hydrocarbons,
And organic efficiency is higher, easy and simple to handle.
The invention discloses the coal tar hydrogenating reaction unit of a kind of quick recovery lighter hydrocarbons, including lighter hydrocarbons recovery section, hydrogenation
Conversion zone；
Described lighter hydrocarbons recovery section include outer tube, intermediate cone, pressure recover section, wherein, described outer tube include leading section and
Rearward end；
Described intermediate cone is entirely located in described outer tube, have be sequentially connected with cone base, cone body, prolongation
Pipe；Axle along radially uniform distribution 6～10 guide vanes of described cone body, described guide vane and described intermediate cone
Angle between to is 30 °～60 °, and described pressure recovers section and is connected with described extension tube and described outer tube back-end portion；
Described hydrogenation reaction section includes raw oil entrance, hydrogen inlet, product oil export, gas outlet；
Described gas outlet couples with described outer tube leading section.
Further, described outer tube includes leading portion, stage casing, back segment, and the size of described leading portion is more than the size of described back segment,
Described stage casing is to connect described leading portion and the conical pipe of back segment.
Further, described outer tube back segment is provided with lighter hydrocarbons outlet, and the outlet of described lighter hydrocarbons recovers section near described pressure.
In the coal tar hydrogenating reaction unit of above-mentioned quick recovery lighter hydrocarbons, described outer tube back segment internal diameter and described outer tube leading portion
The ratio of internal diameter is 1:2～4；Described outer length of tube is 5～12:1 with the ratio of described outer tube leading portion internal diameter；Described conical pipe is with described
The angle of outer tube leading portion is 110 °～160 °.
In the coal tar hydrogenating reaction unit of above-mentioned quick recovery lighter hydrocarbons, before the height of described guide vane and described outer tube
The ratio of section internal diameter is 0.1～0.3: 1；The length of described guide vane is 1: 2～5 with the axial length ratio of described conical pipe.
In the coal tar hydrogenating reaction unit of above-mentioned quick recovery lighter hydrocarbons, before described pressure recovers segment length and described outer tube
The ratio of section internal diameter is 0.5～1:1.
In the coal tar hydrogenating reaction unit of above-mentioned quick recovery lighter hydrocarbons, the cone body part or complete of described intermediate cone
Portion is positioned in described conical pipe, and consistent with its indentation direction；Described extension tube is located fully or partially at described outer tube back segment.
In the coal tar hydrogenating reaction unit of above-mentioned quick recovery lighter hydrocarbons, described cone base is hemispherical, and diameter with
The ratio of described outer tube leading portion internal diameter is 0.6～0.8:1；The ratio of described extension tube external diameter and described outer tube back segment internal diameter be 1:5～
8。
The invention also discloses a kind of coal tar hydrogenating reaction unit utilizing above-mentioned quick recovery lighter hydrocarbons to carry out lighter hydrocarbons and return
The method received, comprises the following steps:
Coal tar, at described hydrogenation reaction section generation hydrocracking reaction, produces cracked gas；
Described cracked gas is transported to described lighter hydrocarbons recovery section by described gas outlet via described outer tube leading portion；
Light hydrocarbon material in described cracked gas forms drop, is flowed out by the outlet of described lighter hydrocarbons.
In the above-mentioned method carrying out lighter hydrocarbons recovery, described cracked gas is more than 340m/s in described prolongation pipeline section speed,
Pressure is 50～60kPa, and temperature is-253～-243 DEG C.
Assembly of the invention can complete the hydrocracking reaction of coal tar, and realizes the recovery of lighter hydrocarbons.Lighter hydrocarbons therein
Exhausting section can utilize the temperature and pressure of cracked gas itself, under intermediate cone wherein and the effect of guide vane, and will
The pressure of cracked gas can be converted into kinetic energy with interior.Extending pipeline section, the speed of gas can reach supersonic speed, and by leading
The centrifugal force produced to blade effect so that the light hydrocarbon component in cracked gas condenses into drop and gets rid of on outer tube wall, by
Lighter hydrocarbons outlet is flowed out.By this lighter hydrocarbons recovery section, the pressure of cracked gas can reduce by 50%.During lighter hydrocarbons recovery, it is not required to
Additionally to supplement energy in device, lighter hydrocarbons recovery efficiency is high.
Accompanying drawing explanation
Fig. 1 is the coal tar hydrogenating reaction unit schematic diagram quickly reclaiming lighter hydrocarbons in the present invention.
Fig. 2 is lighter hydrocarbons recovery section schematic diagram in the present invention.
Reference in accompanying drawing is as follows:
I-hydrogenation reaction section；II-lighter hydrocarbons recovery section；
1-raw oil entrance；2-hydrogen inlet；3-product oil export；4-gas outlet；
5-outer tube；6-intermediate cone；7-pressure recovers section；
8-leading portion；9-conical pipe；10-back segment；
11-lighter hydrocarbons export；
12-cone base；13-cone body；14-extension tube；
15-guide vane.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and its various aspects.But, specific embodiments described below and reality
Executing example is only descriptive purpose rather than limitation of the present invention.
As it is shown in figure 1, the coal tar hydrogenating reaction unit quickly reclaiming lighter hydrocarbons of the present invention includes two parts: hydrogenation is anti-
The section of answering I and lighter hydrocarbons recovery section II, realize the hydrocracking reaction of coal tar in hydrogenation reaction section I, in lighter hydrocarbons recovery section II
The sharp separation realizing lighter hydrocarbons reclaims.
The most as seen from Figure 1, hydrogenation reaction section I be a vertical reactor, bottom and top be hemispherical, middle part for connect the end
Portion and the cylinder at top, comprising: raw oil entrance 1, hydrogen inlet 2, product oil export 3, gas outlet 4.
Raw oil entrance 1 is arranged on the upper end at middle part, and hydrogen inlet 2 is arranged on the bottom at middle part, and product oil export 3 is arranged
In the lower end at middle part, near hydrogen inlet 2, gas outlet 4 is arranged on the top of top hemispherical, in convex shape.
As shown in Figure 2, for the structural representation of lighter hydrocarbons recovery section II, including three parts: outer tube 5, intermediate cone 6, pressure
Power recovers section 7, and structure and relation thereof to described three parts are described separately below:
1. outer tube 5 has leading portion 8, conical pipe 9 (stage casing), a back segment 10, and wherein leading portion 8 and back segment 10 are straight tube, and by
Fig. 2 is visible, and the diameter of leading portion 8 is more than the diameter of rear end 10, and conical pipe 9 is to connect leading portion 8 and the conical pipe of back segment 10.
In order to more clearly describe the detailed description of the invention of this invention, special by the named front end, two ends of above-mentioned outer tube 5
Portion and rearward end, wherein leading section is positioned at the end of leading portion 8, and rearward end is positioned at the end of back segment 10.
2. intermediate cone 6 is made up of the cone base 12 being sequentially connected with, cone body 13, extension tube 14, wherein at the bottom of cone
Portion 12 is the domed bottom of cone, and cone body 13 is cone body, and extension tube 14 is a straight tube.
Intermediate cone 6 is all fixed among outer tube 5, and a part for its cone body 13 is positioned in conical pipe 9, another portion
Divide and be positioned in leading portion 8, and consistent with the indentation direction of conical pipe 9.At cone body 13 radially, near cone base 12
Position be evenly distributed with guide vane 15.
Extension tube 14 is entirely located in back segment 10.
In the present invention, other embodiments between intermediate cone 6 and outer tube 5, also include:
Cone body 13 is entirely located in conical pipe 9, and consistent with the indentation direction of conical pipe 9.
Extension tube 14 is entirely located in back segment 10.
Cone body 13 is entirely located in conical pipe 9, and consistent with the indentation direction of conical pipe 9.
Extension tube 14 part is positioned in back segment 10, and another part is positioned in conical pipe 9.
A part for cone body 13 is positioned in conical pipe 9, and another part is positioned in leading portion 8, and with conical pipe 9
Indentation direction is consistent.
Extension tube 14 part is positioned in back segment 10, and another part is positioned in conical pipe 9.
3. pressure recovery section 7 is connected with the back segment 10 of extension tube 14 and outer tube 5.
The back segment 10 of outer tube 4 is provided with lighter hydrocarbons outlet 12, and lighter hydrocarbons outlet 12 recovers section 7 near pressure.
The gas outlet 4 of hydrogenation reaction section I couples with outer tube 5 leading section of lighter hydrocarbons recovery section II so that in hydrogenation reaction section I
The cracked gas that coal tar hydrocracking produces, it is possible to enter the recovery completing lighter hydrocarbons in lighter hydrocarbons recovery section II.
(2) it is depicted below as the design proportion of each original paper in lighter hydrocarbons recovery section II.
The length of outer tube 5 is 5～12:1 with the internal diameter ratio of leading portion 8, and the internal diameter ratio of the internal diameter of back segment 10 and leading portion 8 is 1:
2～4, the angle between the axial direction of conical pipe 9 and leading portion 8 is 110 °～160 °, and this angle is outer tube leading portion craspedodrome section and cone
The interior angle that shape pipe is formed.
The external diameter of the extension tube 14 of intermediate cone 6 and the internal diameter of back segment 10 are than for 1:5～8.
The drift angle scope of the cone body 13 of intermediate cone 6 is 30 °～60 °, cone base 12 be shaped as hemispherical, should
The diameter of domed bottom is 0.6～0.8:1 with the internal diameter ratio of leading portion 8.
Guide vane 15 is along the radially uniform distribution 6 of cone body 13～10, and guide vane 15 and intermediate cone 6
Angle between Zhou Xiang is 30 °～60 °.
The height of guide vane 15 is 0.1～0.3: 1 with the internal diameter ratio of leading portion 8, the length of guide vane 15 and conical pipe 9
Axial length ratio be 1: 2～5.
It is 0.5～1:1 that pressure recovers the length of section 7 with the internal diameter ratio of leading portion 8.
(3) utilize assembly of the invention to carry out coal tar hydrogenating reaction the method reclaiming wherein lighter hydrocarbons, including following step
Rapid:
Step A, coal tar hydrocracking: add coal tar in device via the raw oil entrance 1 of hydrogenation reaction section I,
And added hydrogen by hydrogen inlet 2, and the hydrocracking reaction of coal tar is carried out in hydrogenation reaction section I, the oil product of generation is by product
Oil export 3 is discharged, and the cracked gas of generation is transported in lighter hydrocarbons recovery section II by gas outlet 4.
In above-mentioned steps, the pressure at hydrogen inlet 2 is 10～24MPa, and the reaction temperature in hydrogenation reaction section I is 380
～460 DEG C, temperature when cracked gas is transported in lighter hydrocarbons recovery section II at gas outlet 4 is 360～420 DEG C.
Step B, lighter hydrocarbons recovery: cracked gas enters in the outer tube 5 of lighter hydrocarbons recovery section II, under the effect of intermediate cone 6,
Owing to internal diameter diminishes, cracked gas being produced throttling, causing the speed of cracked gas to improve becomes high-speed gas.High-speed gas exists
Produce centrifugal force under the effect of guide vane 15, continue to accelerate when cone body 13 and extension tube 14.In extension tube 14, split
The speed solving gas can reach supersonic speed, i.e. more than 340m/s, pressure drop as little as 50～60kPa, centrifugal force reach 100,000 G with
On, temperature is reduced to-253～-243 DEG C.
At the back segment 10 of outer tube 5, the light hydrocarbon material in cracked gas can condense formation drop, under the influence of centrifugal force
Got rid of on the tube wall of back segment 10, then by lighter hydrocarbons outlet 11 outflow lighter hydrocarbons recovery section II, exported lighter hydrocarbons at 11 at lighter hydrocarbons
Temperature is-240～-160 DEG C.
Remaining cracked gas recovers section 7 by pressure, and pressure is increased to 3～8MPa, and temperature is increased to 80～150 DEG C.
In lighter hydrocarbons recovery section II, the pressure of cracked gas and interior can can be exchanged into kinetic energy, speed can reach 3～
5Ma (Ma is speed unit Mach, refers to the ratio of speed and local velocity of sound).After lighter hydrocarbons recovery section II, cracking gas
The pressure of body can reduce by 40%～70%.
Embodiment 1
Hydrogen inlet pressure is 10MPa, and hydrogenation reaction section reaction temperature is 400 DEG C, and cracked gas is temperature at gas outlet
It it is 380 DEG C.Remaining cracked gas recovers section pressure by pressure and is increased to 5MPa, and temperature is increased to 120 DEG C.Lighter hydrocarbons exit is light
Hydrocarbon temperature is-180 DEG C, and C2+ component is flowed out by lighter hydrocarbons outlet.
Wherein lighter hydrocarbons recovery section design proportion is as follows: the domed bottom diameter of middle intercentrum and the ratio of outer tube leading portion internal diameter
Example is 0.8:1；The corner angle of cone body is: 30 °；Conical pipe with outer tube leading portion angle is: 140 °；Outer tube back segment internal diameter with
Outer tube leading portion internal diameter ratio is: 1:4, and outer length of tube with outer tube leading portion internal diameter ratio is: 9:1；Extension tube external diameter and outer tube back segment
Ratio be 1:5；The cone body of middle intercentrum is radially uniform is distributed 6 guide vanes；The length of guide vane and conical pipe
Axial length than for 1:3；The height of guide vane is 0.1:1 with the ratio of outer tube leading portion internal diameter；Guide vane and middle vertebra
Angle between the axial direction of body is 30 °；It is 0.6:1 that pressure recovers the ratio of segment length and outer tube leading portion internal diameter.
After hydrogenated cracking reaction, the composition in detection lighter hydrocarbons exit is as shown in table 1.
Table 1
| C2 | C3 | C4 | C5+ |
| 5.1% | 11.4% | 30.7% | 52.8% |
Embodiment 2
Hydrogen inlet pressure is 20MPa, and hydrogenation reaction section reaction temperature is 400 DEG C, and cracked gas is temperature at gas outlet
It it is 380 DEG C.Remaining cracked gas recovers section pressure by pressure and is increased to 8MPa, and temperature is increased to 120 DEG C.Lighter hydrocarbons exit is light
Hydrocarbon temperature is-205 DEG C, and C2+ component is flowed out by lighter hydrocarbons outlet.
Wherein lighter hydrocarbons recovery section design proportion is as follows: the domed bottom diameter of middle intercentrum and the ratio of outer tube leading portion internal diameter
Example is 0.8:1；The corner angle of cone body is: 60 °；Conical pipe with outer tube leading portion angle is: 140 °；Outer tube back segment internal diameter with
Outer tube leading portion internal diameter ratio is: 1:5, and outer length of tube with outer tube leading portion internal diameter ratio is: 10:1；Extension tube external diameter and outer tube back segment
Ratio be 1:6；The cone body of middle intercentrum is radially uniform is distributed 8 guide vanes；The length of guide vane and conical pipe
Axial length than for 1:3；The height of guide vane is 0.15:1 with the ratio of outer tube leading portion internal diameter；Guide vane and middle vertebra
Angle between the axial direction of body is 45 °；It is 1:1 that pressure recovers the ratio of segment length and outer tube leading portion internal diameter.
After hydrogenated cracking reaction, the composition in detection lighter hydrocarbons exit is as shown in table 2
Table 2
| C2 | C3 | C4 | C5+ |
| 13.3% | 11.4% | 27.77% | 47.6% |
From Tables 1 and 2, apparatus and method of the present invention can C2+ component in efficient recovery cracked gas, and with
The increase (crushing herein refers to that inlet pressure recovers difference and the ratio of inlet pressure of pressure at section with pressure) of crushing, gently
In hydrocarbon component, the ratio of C2 increases.
It should be noted that each embodiment above by reference to described by accompanying drawing is only in order to illustrate rather than restriction originally
The scope of invention, it will be understood by those within the art that, the most right
Amendment that the present invention is carried out or equivalent, all should contain within the scope of the present invention.Additionally, indication unless the context
Outward, the word occurred in the singular includes plural form, and vice versa.It addition, unless stated otherwise, then any embodiment
All or part of can use in conjunction with all or part of of any other embodiments.
Claims (10)
1. a coal tar hydrogenating reaction unit for quick recovery lighter hydrocarbons, including lighter hydrocarbons recovery section, hydrogenation reaction section；
Described lighter hydrocarbons recovery section includes that outer tube, intermediate cone, pressure recover section, and wherein, described outer tube includes leading section and rear end
Portion；
Described intermediate cone is entirely located in described outer tube, have be sequentially connected with cone base, cone body, extension tube；Edge
The radially uniform distribution 6 of described cone body～10 guide vanes, described guide vane and described intermediate cone axial it
Between angle be 30 °～60 °, described pressure recover section be connected with described extension tube and described outer tube back-end portion；
Described hydrogenation reaction section includes raw oil entrance, hydrogen inlet, product oil export, gas outlet；
Described gas outlet couples with described outer tube leading section.
Device the most according to claim 1, it is characterised in that described outer tube includes leading portion, stage casing, back segment, described leading portion
Size more than the size of described back segment, described stage casing is to connect described leading portion and the conical pipe of back segment.
Device the most according to claim 2, it is characterised in that described outer tube back segment be provided with lighter hydrocarbons outlet, and described gently
Hydrocarbon outlet recovers section near described pressure.
Device the most according to claim 2, it is characterised in that described outer tube back segment internal diameter and described outer tube leading portion internal diameter
Ratio is 1:2～4；Described outer length of tube is 5～12:1 with the ratio of described outer tube leading portion internal diameter；Before described conical pipe and described outer tube
The angle of section is 110 °～160 °.
Device the most according to claim 2, it is characterised in that the height of described guide vane and described outer tube leading portion internal diameter
Ratio be 0.1～0.3: 1；The length of described guide vane is 1: 2～5 with the axial length ratio of described conical pipe.
Device the most according to claim 2, it is characterised in that described pressure recovers segment length and described outer tube leading portion internal diameter
Ratio be 0.5～1:1.
Device the most according to claim 2, it is characterised in that the cone body part of described intermediate cone or be entirely located in
In described conical pipe and consistent with its indentation direction；Described extension tube is located fully or partially at described outer tube back segment.
Device the most according to claim 2, it is characterised in that described cone base is hemispherical, and diameter with described outside
The ratio of pipe leading portion internal diameter is 0.6～0.8:1；Described extension tube external diameter is 1:5～8 with the ratio of described outer tube back segment internal diameter.
9. utilize the described device of one of claim 1-8 to reclaim a method for lighter hydrocarbons in coal tar, comprise the following steps:
Coal tar, at described hydrogenation reaction section generation hydrocracking reaction, produces cracked gas；
Described cracked gas is transported to described lighter hydrocarbons recovery section by described gas outlet via described outer tube leading portion；
Light hydrocarbon material in described cracked gas forms drop, is flowed out by the outlet of described lighter hydrocarbons.
Method the most according to claim 9, it is characterised in that described cracked gas is big in described prolongation pipeline section speed
In 340m/s, pressure is 50～60kPa, and temperature is-253～-243 DEG C.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201215413Y (en) * | 2008-04-30 | 2009-04-01 | 大连理工大学 | Damped opposite flushing type air wave refrigerator |
| CN103695036A (en) * | 2013-12-31 | 2014-04-02 | 上海新佑能源科技有限公司 | Medium and low temperature coal tar processing method |
| CN104832226A (en) * | 2015-03-31 | 2015-08-12 | 李大鹏 | Coal-to-liquids and gas generating cogeneration apparatus and method |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201215413Y (en) * | 2008-04-30 | 2009-04-01 | 大连理工大学 | Damped opposite flushing type air wave refrigerator |
| CN103695036A (en) * | 2013-12-31 | 2014-04-02 | 上海新佑能源科技有限公司 | Medium and low temperature coal tar processing method |
| CN104832226A (en) * | 2015-03-31 | 2015-08-12 | 李大鹏 | Coal-to-liquids and gas generating cogeneration apparatus and method |
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