CN109880658A - A kind of coke tar recovery system and technique - Google Patents
A kind of coke tar recovery system and technique Download PDFInfo
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- CN109880658A CN109880658A CN201910270943.9A CN201910270943A CN109880658A CN 109880658 A CN109880658 A CN 109880658A CN 201910270943 A CN201910270943 A CN 201910270943A CN 109880658 A CN109880658 A CN 109880658A
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- heavy
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- 238000011084 recovery Methods 0.000 title claims abstract description 177
- 239000011285 coke tar Substances 0.000 title claims abstract description 13
- 238000000034 method Methods 0.000 title description 17
- 239000011269 tar Substances 0.000 claims abstract description 444
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000002826 coolant Substances 0.000 claims abstract description 28
- 238000004891 communication Methods 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 119
- 238000003860 storage Methods 0.000 claims description 56
- 239000002351 wastewater Substances 0.000 claims description 53
- 239000000047 product Substances 0.000 claims description 49
- 238000004064 recycling Methods 0.000 claims description 36
- 238000001816 cooling Methods 0.000 claims description 35
- 239000007921 spray Substances 0.000 claims description 33
- 230000008676 import Effects 0.000 claims description 30
- 239000002918 waste heat Substances 0.000 claims description 20
- 238000005235 decoking Methods 0.000 claims description 19
- 239000012716 precipitator Substances 0.000 claims description 16
- 238000006392 deoxygenation reaction Methods 0.000 claims description 8
- 239000013589 supplement Substances 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000004781 supercooling Methods 0.000 claims description 2
- 239000002641 tar oil Substances 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000003921 oil Substances 0.000 description 312
- 239000003034 coal gas Substances 0.000 description 5
- 239000011280 coal tar Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- KQTVWCSONPJJPE-UHFFFAOYSA-N etridiazole Chemical compound CCOC1=NC(C(Cl)(Cl)Cl)=NS1 KQTVWCSONPJJPE-UHFFFAOYSA-N 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000010009 beating Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000011286 gas tar Substances 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 230000011218 segmentation Effects 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a kind of coke tar recovery systems, including tar classification recovery system A, tar light oil depth recovery system B, residual neat recovering system C and grading stocking system D；Tar is classified the oil product inlet communication of the oil product outlet and residual neat recovering system C of recovery system A, the oil product outlet grading stocking system D of the oil product outlet and tar light oil depth recovery system B of residual neat recovering system C；Residual neat recovering system C offers cooling medium entrance, the steam inlet of the cooling medium outlet tar light oil depth recovery system B of residual neat recovering system C；The gas vent that tar is classified recovery system A is connected to tar light oil depth recovery system B, the cooling medium inlet of the gas vent connection tar classification recovery system A of tar light oil depth recovery system B；It solves the problems, such as that tar is separated from water hardly possible, improves the quality of tar product；Thermal energy obtains effective reuse, and system energy consumption is effectively reduced, and system water consume is extremely low, water-saving result is significant.
Description
Technical field
The invention belongs to technical field of coal chemical industry, and in particular to a kind of coke tar recovery system and technique.
Background technique
Main high value added product of the coal tar as pyrolysis of coal technology, yield and quality are to influence pyrolysis of coal technology warp
The principal element of Ji property.The way of recycling of coal tar mainly includes Dry recovery and hydrometallurgic recovery.Relative maturity and industry at present
Change degree is higher to mostly use wet process, and vertical heater pyrolytic technique is mainly using the " washing for taking water (ammonium hydroxide) as detergent
Method ".Water scrubber mainly includes spray column, venturi tower, impact bubble cleaning tower and packed tower etc..The essence of washing is that cooling is made
With, there is good removal effect for tar heavy oil, but operation temperature is lower, can generate stickiness particle and salt causes to tie
Coke blocks pipeline and valve.The dissolution and elution of the highly polar achievable heteroatom class tar of water, but cause tar washed wastewater at
For complicated suspension containing phenol, processing cost is high；The highly polar of water does not have compatibility to hydro carbons tar, thus removal effect is very
Difference, and this kind of tar actually controls the dew point of tar in pyrolysis gas.Therefore, from the perspective of degree of purification and the feature of environmental protection,
WATER-WASHING METHOD cannot obtain satisfied tar recovering effect.
The method of oil base recycling tar is the compatibility using cool oils absorbent and tar, that is, model moral
Magnificent power effect, therefore have the advantages that more to be avoided that the pollution problem of phenol wastewater except washing oil, and light hydrocarbon coke can be improved
Gas tar dew point can be down to operation temperature or less by oily removal effect, the presence of absorption.But current oil wash technique
There is a problem of corresponding not yet solving.Firstly, existing " oil wash method " is generally two cooling techniques for arriving three-level, level-one is cooled down cold
But oil is usually beating circulation higher than 200 DEG C or more, and secondary response easily occurs in the higher situation of temperature and forms coking for coal tar,
Influence the quality and yield of tar；Secondly the coal tar oil density of mixed collection approaches with the density of water 1.05 or so, is difficult reality
Existing water-oil separating, is unfavorable for the subsequent use of coal tar；The temperature of third, cooling tail end is controlled at 50 DEG C or so more, and most
Tar recycling operates under the conditions of tiny structure, is limited by vapor liquid equilibrium, a large amount of light components still fail to recycle, and influence downstream and set
Standby stable operation and coal gas further use；4th, system uses a large amount of recirculated cooling waters, and heat fails to efficiently use.
Summary of the invention
In order to solve problems of the prior art, the invention discloses the present invention in order to solve current tar recycling
The problems such as system tar rate of recovery is low, the consumption of system cooling capacity is big, tar sensible heat does not utilize, provides a kind of low energy consumption high yield tar
Recovery system and technique.
To achieve the goals above, the technical solution adopted by the present invention is that, a kind of coke tar recovery system, including tar are classified
Recovery system, tar light oil depth recovery system, residual neat recovering system and grading stocking system；Tar classification recycling system
The oil product inlet communication of the oil product outlet and residual neat recovering system of system, the oil product outlet of residual neat recovering system and tar light oil depth
The oil product outlet grading stocking system of recovery system；Residual neat recovering system offers cooling medium entrance, and waste heat returns
The steam inlet of the cooling medium outlet tar light oil depth recovery system of receipts system；The gas of tar classification recovery system
Outlet tar light oil depth recovery system, the gas vent connection tar classification recycling system of tar light oil depth recovery system
The cooling medium inlet of system.
Tar classification recovery system includes asphalitine recovery tower, heavy tar recovery tower and tar light oil recovery tower,
In, the outlet of asphalitine recovery tower top gas is connected with heavy tar recovery tower import, heavy tar recovery tower top gas
Outlet is connected with tar light oil recovery tower import；The outlet of tar light oil recovery tower connects tar light oil depth recovery system；
The outlet of asphalitine recovery tower, heavy tar recovery tower and tar light oil recovery tower is all connected with residual neat recovering system.
Tar light oil depth recovery system includes low temperature recovery tower and electrical tar precipitator, the connection of low temperature recovery tower gas vent
The oil product outlet of electrical tar precipitator, low temperature recovery tower and electrical tar precipitator is connected to grading stocking system；Electrical tar precipitator
Top opens up gas vent, the cooling medium inlet of the gas vent connection tar classification recovery system.
Residual neat recovering system includes the oxygen-eliminating device, tar light oil pans, heavy coke being sequentially communicated along cooling medium flow direction
Oily pans and asphalitine pans；The steam inlet of the cooling medium outlet low temperature recovery tower of asphalitine pans；
The outlet of low temperature recovery tower steam condensate is connected to oxygen-eliminating device；Be provided on the pipeline that oxygen-eliminating device is connected to tar light oil pans to
Water pump.
The outlet of tar light oil recovery tower connects roots blower, the import of the outlet connection low temperature recovery tower of roots blower；
The oil product outlet connection asphalitine pans of asphalitine recovery tower, the oil product outlet of heavy tar recovery tower connect in heavy tar
Between tank, tar light oil recovery tower oil product outlet connection tar light oil pans.
Grading stocking system include mutually independent asphalitine storage tank, heavy tar storage tank, tar light oil storage tank with
And wastewater storage tank；The oil outlet of asphalitine pans connects asphalitine storage tank, and the outlet of heavy tar pans oil product is divided into two-way,
It is connected all the way with heavy tar recycling tower cooler absorbing medium import, heavy tar in another way and grading stocking system
The import of storage tank is connected；The outlet of tar light oil pans oil product is divided into two-way, wherein cold with tar light oil recovery tower all the way
But absorbing medium inlet communication, the inlet communication of another way and tar light oil storage tank, tar light oil pans wastewater outlet and useless
Water tank inlet connection heavy tar pans wastewater outlet is connected with wastewater storage tank import in grading stocking system.
Heavy tar pump is provided between heavy tar recycling tower bottom oil product outlet and heavy tar pans；Lightweight is burnt
Tar light oil pump is provided between oil recycling tower bottom oil product outlet and tar light oil pans.
A kind of tar recovery process, mixed oil and gas obtain sensible heat asphalitine to be recycled after supercooling and except pitch miscellas
Gas, except pitch mixed oil and gas obtains sensible heat heavy tar to be recycled and except heavy tar mixed oil and gas after cooling；
The waste heat of sensible heat asphalitine to be recycled obtains asphalitine after recycling, recycles and stores to asphalitine；
Heavy tar, spray heavy tar and the upper waste water of oil are obtained after the waste heat of sensible heat heavy tar to be recycled is recovered；
Heavy tar is recycled, waste water carries out waste water recycling device on oil；
Except heavy tar mixed oil and gas obtains sensible heat tar light oil to be recycled and level-one except tar light oil mixes after cooling
Oil gas；
It is lower useless that spray tar light oil, the first tar light oil and oil are obtained after the waste heat recycling of sensible heat tar light oil to be recycled
Water；Waste water recycling device is carried out to waste water under oil；First tar light oil is recycled；
Level-one removes tar light oil mixed oil and gas afterwards except tar light oil mixed oil and gas is pressurized for positive pressure level-one, and positive pressure level-one is removed
The second tar light oil and second level are obtained after tar light oil mixed oil and gas depth is cooling except tar light oil mixed oil and gas, second level is except light
Matter tar mixed oil and gas traps to obtain third tar light oil and decoking oil gas by tar droplet, to the second tar light oil and the
Three tar light oils carry out recycling storage.
Decoking oil gas and mixed oil and gas obtain heating decoking oil gas after carrying out heat exchange；Supplement desalted water is obtained through deoxygenation
Deaerated water, deaerated water are pressurized successively to sensible heat tar light oil to be recycled, sensible heat heavy tar to be recycled and sensible heat to be recycled
Asphalitine is cooled down, and respectively corresponds to obtain level-one heat exchange hot water, second level heat exchange steam and the friendship of three-level heat after heat exchange
Change steam, the three-level heat exchange steam power required when cooling as the second tar light oil.
Steam condensate is formed after three-level heat exchange steam output power, steam condensate is after deoxygenation together with deaerated water
It is overpressurized successively cold to the progress of sensible heat tar light oil to be recycled, sensible heat heavy tar to be recycled and sensible heat asphalitine to be recycled
But；
Except pitch mixed oil and gas is cooling using spray heavy tar, except heavy tar mixed oil and gas is using spray tar light oil
It is cooling.
Compared with prior art, the present invention at least has the advantages that
1, tar product high income, quality are good: technical solution of the present invention increases tar light oil compared to traditional technology
Exhausting section effectively improves product yield, while the Product recycling mode for being fractionated segmentation can effectively avoid tar and be separated from water hardly possible
Problem, it is ensured that the quality of tar product；
2, it is connected using the product that recovery system of the present invention and technique recycle convenient for downstream, lengthening manufacturing chain: for
Asphalitine, heavy tar and the tar light oil product stored respectively after tar recycling can simplify subsequent tar production boiling point cutting
Process, for being pyrolyzed coal gas, tar residual volume is substantially reduced in the pyrolysis coal gas by tar light oil recovery system, is conducive to heat
Solve the further utilization of coal gas；
3, thermal energy obtains effective reuse, and system energy consumption is effectively reduced, and by the utilization step by step of energy, it is mixed effectively to recycle high temperature
A large amount of sensible heat byproduct steams of oil gas are closed, and provide low temperature power using byproduct steam, are reduced significantly in order to effectively recycle
Energy consumption needed for light components and other power consumptions；
4, system water consume is extremely low, water-saving result is significant: deaerated water is by recycling tar heat pair in technique of the present invention
Producing steam, byproduct steam, which condenses to form steam condensate and further return to oxygen-eliminating device as cooling medium in low temperature recyclable device, to be made
With, it is only necessary to the closed cycle that public work water can be then formed by the extraneous minimal amount of desalted water of supplement avoids circulation
A large amount of losses of water reduce system water consume, avoid cooling tower or air-cooled investment, with also alleviating general rich coal resources
Area, water resource relative scarcity recycle the biggish contradiction of water loss.
Detailed description of the invention
Fig. 1 is present invention process flow diagram；
Fig. 2 is tar recovery process system schematic of the present invention；
In attached drawing, A- tar is classified recovery system B- tar light oil depth recovery system C- residual neat recovering system D- product point
Grade stocking system；
101- asphalitine recovery tower, 102- heavy tar recovery tower, 103- tar light oil recovery tower, 401- roots blower,
601- low temperature recovery tower, 501- electrical tar precipitator, 201- asphalitine storage tank, 202- heavy tar storage tank, the storage of 203- tar light oil
Tank, 204- wastewater storage tank, 205- asphalitine pans 206- heavy tar pans 207- tar light oil pans, 208- deoxygenation
Device, 301- heavy tar pump, 302- tar light oil pump, 303- feed pump, 01- high temperature mixed oil and gas, 02- remove pitch miscella
Gas, 03- remove heavy tar mixed oil and gas, and 04- level-one removes tar light oil mixed oil and gas, and 05- positive pressure level-one is mixed except tar light oil
Oil gas, 06- second level remove tar light oil mixed oil and gas, 07- decoking oil gas, 08- high temperature decoking oil gas, 09- sensible heat to be recycled
Asphalitine, 10- asphalitine, 11- sensible heat heavy tar to be recycled, waste water on 12- oil, 13- heavy tar, it is burnt that 14- sprays heavy
Oil, 15- sensible heat tar light oil to be recycled, waste water under 16- oil, 17- spray tar light oil, the first tar light oil of 18-, 19- second
Tar light oil, 20- third tar light oil, 21- steam condensate, 22- deaerated water, 23- supplement desalted water, 24- level-one heat exchange heat
Water, 25- second level heat exchange steam, 26- three-level heat exchange steam.
Specific embodiment
Combined with specific embodiments below and attached drawing the present invention will be described in detail.
A kind of coke tar recovery system, including tar classification recovery system A, tar light oil depth recovery system B, waste heat recycling
System C and grading stocking system D；Tar be classified the oil product outlet of recovery system A and the oil product of residual neat recovering system C into
Mouth connection, the oil product outlet and the oil product outlet grading of tar light oil depth recovery system B of residual neat recovering system C are stored up
Deposit system D；Residual neat recovering system C offers cooling medium entrance, and the cooling medium outlet lightweight of residual neat recovering system C is burnt
The steam inlet of oily depth recovery system B；The gas vent that tar is classified recovery system A is connected to tar light oil depth recovery system
The cooling medium inlet of the gas vent connection tar classification recovery system A of B, tar light oil depth recovery system B.
Wherein, tar classification recovery system includes that asphalitine recovery tower 101, heavy tar recovery tower 102 and lightweight are burnt
Oily recovery tower 103；The outlet of 101 top gas of asphalitine recovery tower is connected with 102 import of heavy tar recovery tower, heavy tar
The outlet of 102 top gas of recovery tower is connected with 103 import of tar light oil recovery tower；
Tar light oil depth recovery system includes roots blower 401, low temperature recovery tower 601 and electrical tar precipitator 501；Roots
The outlet of blower 401 is connected with 601 entrance of low temperature recovery tower, 601 gas vent of low temperature recovery tower and 501 import of electrical tar precipitator
It is connected；
Residual neat recovering system includes oxygen-eliminating device 208, feed pump 303, tar light oil pans 207, heavy tar pans
206 and asphalitine pans 205；The deoxygenation water out of oxygen-eliminating device 208 is connected with 303 import of feed pump, and feed pump 303 goes out
Mouth is connected with 207 cooling medium inlet of tar light oil pans, and the outlet of 207 cooling medium of tar light oil pans and heavy are burnt
Oily 206 cooling medium inlet of pans is connected, the outlet of 206 cooling medium of heavy tar pans and asphalitine pans 205
Cooling medium inlet is connected；301 outlet of heavy tar pump is connected with the 206 oil product import of heavy tar pans, and lightweight is burnt
The outlet of oil pump 302 is connected with the 207 oil product import of tar light oil pans.
Grading stocking system include asphalitine storage tank 201, heavy tar storage tank 202, tar light oil storage tank 203 and
Wastewater storage tank 204.
Tar is classified in the outlet of 101 bottom oil product of recovery system studies on asphaltene recovery tower and residual neat recovering system studies on asphaltene
Between 205 oil product import of tank be connected, 102 bottom oil product of heavy tar recovery tower outlet with residual neat recovering system C in heavy tar
301 imports are pumped to be connected, 103 bottom oil product of tar light oil recovery tower outlet with residual neat recovering system C in tar light oil pump 302 into
Mouthful be connected, the outlet of 103 top gas of tar light oil recovery tower and roots blower 401 in tar light oil depth recovery system B into
Mouth is connected.
The outlet of 601 oil product of low temperature recovery tower, the outlet of 501 oil product of electrical tar precipitator and production in tar light oil depth recovery system
203 import of tar light oil storage tank is connected in product classification stocking system；501 gas vent of electrical tar precipitator and tar classification are recycled
101 cooling medium inlet of system studies on asphaltene recovery tower is connected, and the outlet of 601 steam condensate of low temperature recovery tower is with waste heat recycling
208 import of oxygen-eliminating device is connected in system.
The outlet of 206 oil product of heavy tar pans is divided into two-way in residual neat recovering system, is classified recycling system with tar all the way
The cooling absorbing medium import of heavy tar recovery tower 102 is connected in system, and heavy is burnt in another way and grading stocking system
The import of oil tank 202 is connected, wastewater storage tank in 206 wastewater outlet of heavy tar pans and grading stocking system
204 imports are connected；The outlet of 207 oil product of tar light oil pans is divided into two-way, is classified lightweight in recovery system with tar all the way
The cooling absorbing medium import of tar recovery tower 103 is connected, tar light oil storage tank 203 in another way and grading stocking system
Import is connected, and 207 wastewater outlet of tar light oil pans is connected with 204 import of wastewater storage tank in grading stocking system
It connects；The outlet of 205 cooling medium of asphalitine pans and 601 steam inlet phase of low temperature recovery tower in tar light oil depth recovery system
Connection, the outlet of 205 oil product of asphalitine pans are connected with 201 import of grading stocking system studies on asphaltene storage tank.
450~700 DEG C of high temperature mixed oil and gas 01 enters asphalitine recovery tower 101, obtains 300~360 DEG C after cooling
Sensible heat asphalitine 09 and 300~360 DEG C to be recycled remove pitch mixed oil and gas 02, sensible heat asphalitine 09 to be recycled enter pitch
Matter pans 205, into heavy tar recovery tower 102, obtained after spray heavy tar 14 is cooling 170~210 DEG C wait return
That receives sensible heat heavy tar 11 and 170~210 DEG C removes heavy tar mixed oil and gas 03, and sensible heat heavy tar to be recycled 11 is through heavy
Tar pump 301 enters heavy tar pans 206, except heavy tar mixed oil and gas 03 enters tar light oil recovery tower 103, through spraying
The sensible heat tar light oil 15 to be recycled and level-one that 50~80 DEG C are obtained after leaching tar light oil 17 is cooling are except tar light oil mixed oil and gas
04, sensible heat tar light oil 15 to be recycled enters tar light oil pans 207 through tar light oil pump 302, and level-one is mixed except tar light oil
It closes oil gas 04 and is pressurised into positive pressure level-one except tar light oil mixed oil and gas 05 through roots blower 401, pressure is 8~15kPa, positive pressure one
Grade obtains tar light oil 19 and second level except tar light oil mixed oil and gas 05 is cooled to 10~25 DEG C through 601 depth of low temperature recovery tower
Except tar light oil mixed oil and gas 06, second level removes tar light oil mixed oil and gas 06 and obtains 20 He of tar light oil through electrical tar precipitator 501
Decoking oil gas 07, decoking oil gas 07 enter asphalitine recovery tower 101 and are used as cooling medium, and it is de- that high temperature is obtained after heat exchange
Tar coal gas 08；The steam condensate 21 and supplement desalted water 23 of low temperature recovery tower 601 obtain deaerated water 22, deoxygenation through oxygen-eliminating device 208
Water 22 passes sequentially through tar light oil pans 207, heavy tar pans 206 and asphalitine pans through feed pump 303
205, respectively obtain level-one heat exchange hot water 24, second level heat exchange steam 25 and three-level heat exchange steam 26 after heat exchange, three
Grade heat exchange steam 26 enters the low temperature environment that low temperature recovery tower 601 provides 8~15 DEG C；Sensible heat asphalitine to be recycled 09 is in pitch
Asphalitine 10 is obtained in matter pans 205 after waste heat recycling, and enters asphalitine storage tank 201；Sensible heat heavy tar 11 to be recycled
Heavy tar 13, spray heavy tar 14 and the upper waste water 12 of oil, heavy are obtained after waste heat recycling in heavy tar pans 206
Tar 13 enters heavy tar storage tank 202, and spray heavy tar 14 enters heavy tar recovery tower 102, and waste water 12 enters on oil
Wastewater storage tank 204；Sensible heat tar light oil 15 to be recycled obtains spray tar light oil in tar light oil storage tank 207 after waste heat recycling
17, the first tar light oil 18 and the lower waste water 16 of oil, the lower waste water 16 of oil enter wastewater storage tank 204, and spray tar light oil 17 enters light
Matter tar recovery tower 103, the first tar light oil 18, the second tar light oil 19 enter tar light oil with third tar light oil 20 together
Storage tank 203；First tar light oil 18 of the present invention, the second tar light oil 19 are identical as the essence of third tar light oil 20, and "
One ", " second " and " third " only understands technique and system of the present invention to distinguish for help.
Embodiment:
Embodiment 1:
Parameter is 550 DEG C, the high temperature mixed oil and gas 01 of 3KPa enters asphalitine recovery tower 101, obtains about 360 after cooling
DEG C sensible heat asphalitine 09 to be recycled and about 360 DEG C remove pitch mixed oil and gas 02, sensible heat asphalitine 09 to be recycled enter pitch
Matter pans 205, -1KPa enter heavy tar recovery tower 102 except pitch mixed oil and gas 02, after spray heavy tar 14 is cooling
Obtain about 210 DEG C sensible heat heavy tar 11 to be recycled and about 210 DEG C except heavy tar mixed oil and gas 03, sensible heat weight to be recycled
Matter tar 11 enters heavy tar pans 206 through heavy tar pump 301, and -5KPa is light except heavy tar mixed oil and gas 03 enters
Matter tar recovery tower 103 obtains about 50 DEG C of sensible heat tar light oil 15 to be recycled and level-one after spray tar light oil 17 is cooling
Except tar light oil mixed oil and gas 04, sensible heat tar light oil 15 to be recycled enters tar light oil pans through tar light oil pump 302
207, level-one removes tar light oil mixed oil and gas 05 except tar light oil mixed oil and gas 04 is pressurised into positive pressure level-one through roots blower 401,
Pressure is about 10kPa, and positive pressure level-one is obtained except tar light oil mixed oil and gas 05 is cooled to 8~15 DEG C through 601 depth of low temperature recovery tower
Tar light oil mixed oil and gas 06 is removed to tar light oil 19 and second level, second level is except tar light oil mixed oil and gas 06 is through electrical tar precipitator
501 obtain tar light oil 20 and decoking oil gas 07, and decoking oil gas 07 enters asphalitine recovery tower 101 and is used as cooling medium,
High temperature decoking oil gas 08 is obtained after heat exchange exports battery limit (BL)；The steam condensate 21 and supplement desalted water of low temperature recovery tower 601
23 obtain deaerated water 22 through oxygen-eliminating device 208, and deaerated water 22 passes sequentially through tar light oil pans 207, heavy tar through feed pump 303
Pans 206, asphalitine pans 205 respectively obtain level-one heat exchange hot water 24, second level heat exchange steam after heat exchange
25, the middle pressure three-level heat exchange steam 26 of three-level heat exchange steam 26,3.5MPa is mentioned into steam-sprayed low temperature recovery tower 601
For 8~15 DEG C of low temperature environment, medium pressure heat exchange steam is steam of the pressure in 2.5~6MPa；Sensible heat drip to be recycled
Green matter 09 obtains asphalitine 10 in asphalitine pans 205 after waste heat recycling, and enters asphalitine storage tank 201, to be recycled aobvious
Hot heavy tar 11 obtains heavy tar 13, spray heavy tar 14 and oil in heavy tar pans 206 after waste heat recycling
Upper waste water 12, heavy tar 13 enter heavy tar storage tank 202, and spray heavy tar 14 enters heavy tar recovery tower 102, oil
Upper waste water 12 enters wastewater storage tank 204；Sensible heat tar light oil 15 to be recycled obtains after waste heat recycling in tar light oil storage tank 207
The lower waste water 16 of tar light oil 17, the first tar light oil 18 and oil is sprayed, the lower waste water 16 of oil enters wastewater storage tank 204, sprays lightweight
Tar 17 enters tar light oil recovery tower 103, and the first tar light oil 18, the second tar light oil 19 and third tar light oil 20 are together
Into tar light oil storage tank 203.
Embodiment 2
Parameter is 450~700 DEG C, the high temperature mixed oil and gas 01 of 3KPa enters asphalitine recovery tower 101, cooling through deaerated water
Obtain afterwards about 360 DEG C sensible heat asphalitine 09 to be recycled and about 360 DEG C except pitch mixed oil and gas 02, and by-product mesohigh steams
Vapour, sensible heat asphalitine 09 to be recycled enter asphalitine pans 205, and -1KPa is returned except pitch mixed oil and gas 02 enters heavy tar
Tower 102 is received, the sensible heat heavy tar 11 to be recycled for obtaining after spray heavy tar 14 is cooling about 210 DEG C and about 210 DEG C remove
Heavy tar mixed oil and gas 03, sensible heat heavy tar 11 to be recycled enter heavy tar pans 206 through heavy tar pump 301 ,-
5KPa enters tar light oil recovery tower 103 except heavy tar mixed oil and gas 03, obtains about 50 after spray tar light oil 17 is cooling
DEG C sensible heat tar light oil 15 to be recycled and level-one remove tar light oil mixed oil and gas 04, sensible heat tar light oil to be recycled 15 is through lightweight
Tar pump 302 enters tar light oil pans 207, and level-one is positive except tar light oil mixed oil and gas 04 pressurizes through roots blower 401
Level-one is pressed to remove tar light oil mixed oil and gas 05, pressure is about 10kPa, and positive pressure level-one is except tar light oil mixed oil and gas 05 is through low temperature time
Receipts 601 depth of tower is cooled to 8~15 DEG C and obtains tar light oil 19 and second level except tar light oil mixed oil and gas 06, and second level removes lightweight
Tar mixed oil and gas 06 obtains tar light oil 20 and decoking oil gas 07 through electrical tar precipitator 501, and decoking oil gas 07 is as production
Product export battery limit (BL)；The steam condensate 21 and supplement desalted water 23 of low temperature recovery tower 601 obtain deaerated water 22, deoxygenation through oxygen-eliminating device 208
Water 22 divides through feed pump 303 for two-way, passes sequentially through tar light oil pans 207 all the way, heavy tar pans 206 obtain two
Grade heat exchange steam 25, second level heat exchange steam 25 enter power of the oxygen-eliminating device 208 as oxygen-eliminating device 208；Another way deaerated water
22, which enter asphalitine pans 205, exchanges heat, and enters steam absorption low temperature recovery tower 601 through the middle pressure steam that heat exchange obtains and mentions
For 8~15 DEG C of low temperature environment, is got rid of outside after oil cooler further cools down again by cooled asphalitine and enter asphalitine
Storage tank 201；Sensible heat heavy tar 11 to be recycled obtains heavy tar 13, spray in heavy tar pans 206 after waste heat recycling
Heavy tar 14 and the upper waste water 12 of oil are drenched, heavy tar 13 enters heavy tar storage tank 202, and spray heavy tar 14 enters heavy
Tar recovery tower 102, waste water 12 enters wastewater storage tank 204 on oil；Sensible heat tar light oil 15 to be recycled is in tar light oil storage tank 207
The lower waste water 16 of spray tar light oil 17, the first tar light oil 18 and oil is obtained after middle waste heat recycling, the lower waste water 16 of oil enters waste water
Storage tank 204, spray tar light oil 17 enter tar light oil recovery tower 103, the first tar light oil 18, the second tar light oil 19 and the
Three tar light oils 20 enter tar light oil storage tank 203 together.
Embodiment 3:
Parameter is 450~700 DEG C, the high temperature mixed oil and gas 01 of 3KPa enters asphalitine recovery tower 101, through decoking oil gas
07 it is cooling after obtain about 360 DEG C of sensible heat asphalitine 09 to be recycled and about 360 DEG C are removed pitch mixed oil and gas 02, sensible heat to be recycled
Asphalitine 09 enters pitch pans 205；- 1KPa enters heavy tar recovery tower 102 except pitch mixed oil and gas 02, through spray weight
The sensible heat heavy tar 11 to be recycled that about 210 DEG C are obtained after matter tar 14 is cooling and about 210 DEG C remove heavy tar mixed oil and gas
03, sensible heat heavy tar 11 to be recycled enters heavy tar pans 206 through heavy tar pump 301, and -5KPa is mixed except heavy tar
It closes oil gas 03 and enters tar light oil recovery tower 103, it is light that about 50 DEG C of sensible heat to be recycled is obtained after spray tar light oil 17 is cooling
Matter tar 15 and level-one remove tar light oil mixed oil and gas 04, and sensible heat tar light oil 15 to be recycled enters light through tar light oil pump 302
Matter tar pans 207, level-one remove tar light oil except tar light oil mixed oil and gas 04 is pressurised into positive pressure level-one through roots blower 401
Mixed oil and gas 05, pressure are about 10kPa, and positive pressure level-one is cooling through 601 depth of low temperature recovery tower except tar light oil mixed oil and gas 05
Tar light oil 19 and second level are obtained except tar light oil mixed oil and gas 06 to 8~15 DEG C, and second level removes tar light oil mixed oil and gas 06
Tar light oil 20 and decoking oil gas 07 are obtained through electrical tar precipitator 501, decoking oil gas 07 enters asphalitine recovery tower 101 and makees
For cooling medium, high temperature decoking oil gas 08 is obtained after heat exchange and exports battery limit (BL)；The steam condensate 21 of low temperature recovery tower 601 with
Supplement desalted water 23 through oxygen-eliminating device 208 deaerated water 22, deaerated water 22 divide through feed pump 303 for two-way, pass sequentially through all the way light
Matter tar pans 207, heavy tar pans 206 obtain second level heat exchange steam 25, and second level heat exchange steam 25, which enters, to be removed
Power of the oxygen device 208 as oxygen-eliminating device 208；Another way deaerated water 22 enters asphalitine pans 205 and exchanges heat, and obtains through heat exchange
Middle pressure steam enter steam absorption low temperature recovery tower 601 8~15 DEG C of low temperature environment be provided, by cooled asphalitine
It is got rid of outside after oil cooler further cools down again and enters asphalitine storage tank 201；Sensible heat heavy tar to be recycled 11 is in heavy tar
Heavy tar 13, spray heavy tar 14 and the upper waste water 12 of oil, heavy tar 13 are obtained in pans 206 after waste heat recycling to enter
Heavy tar storage tank 202, spray heavy tar 14 enter heavy tar recovery tower 102, and waste water 12 enters wastewater storage tank on oil
204；Sensible heat tar light oil 15 to be recycled obtains spray tar light oil 17, first in tar light oil storage tank 207 after waste heat recycling
Tar light oil 18 and the lower waste water 16 of oil, the lower waste water 16 of oil enter wastewater storage tank 204, and spray tar light oil 17 enters tar light oil and returns
Tower 103 is received, the first tar light oil 18, the second tar light oil 19 enter tar light oil storage tank 203 with third tar light oil 20 together.
Claims (10)
1. a kind of coke tar recovery system, which is characterized in that including tar classification recovery system (A), tar light oil depth recycling system
System (B), residual neat recovering system (C) and grading stocking system (D)；Tar be classified recovery system (A) oil product outlet with
The oil product inlet communication of residual neat recovering system (C), the oil product outlet of residual neat recovering system (C) and tar light oil depth recovery system
(B) oil product outlet grading stocking system (D)；Residual neat recovering system (C) offers cooling medium entrance, and waste heat returns
The steam inlet of the cooling medium outlet tar light oil depth recovery system (B) of receipts system (C)；Tar is classified recovery system
(A) gas vent is connected to tar light oil depth recovery system (B), and the gas vent of tar light oil depth recovery system (B) connects
The cooling medium inlet of logical tar classification recovery system (A).
2. coke tar recovery system according to claim 1, which is characterized in that it includes pitch that tar, which is classified recovery system (A),
Matter recovery tower (101), heavy tar recovery tower (102) and tar light oil recovery tower (103), wherein asphalitine recovery tower
(101) top gas outlet is connected with heavy tar recovery tower (102) import, heavy tar recovery tower (102) top gas
Outlet is connected with tar light oil recovery tower (103) import；The outlet of tar light oil recovery tower (103) connects tar light oil depth
Recovery system (B)；Asphalitine recovery tower (101), heavy tar recovery tower (102) and tar light oil recovery tower (103) go out
Mouth is all connected with residual neat recovering system (C).
3. coke tar recovery system according to claim 2, which is characterized in that tar light oil depth recovery system (B) includes
Low temperature recovery tower (601) and electrical tar precipitator (501), low temperature recovery tower (601) gas vent are connected to electrical tar precipitator (501),
Low temperature recovery tower (601) is connected to grading stocking system (D) with the outlet of the oil product of electrical tar precipitator (501)；Electrically trapped tar oil
Gas vent, the cooling medium inlet of gas vent connection tar classification recovery system (A) are opened up at the top of device (501).
4. coke tar recovery system according to claim 2, which is characterized in that residual neat recovering system (C) includes being situated between along cooling
Mass flow is to oxygen-eliminating device (208), tar light oil pans (207), heavy tar pans (206) and the asphalitine being sequentially communicated
Pans (205)；The steam inlet of the cooling medium outlet low temperature recovery tower (601) of asphalitine pans (205)；Low temperature
The outlet of recovery tower (601) steam condensate is connected to oxygen-eliminating device (208)；Oxygen-eliminating device (208) is connected to tar light oil pans (207)
Pipeline on be provided with feed pump (303).
5. coke tar recovery system according to claim 4, which is characterized in that the outlet of tar light oil recovery tower (103) connects
It connects roots blower (401), the import of outlet connection low temperature recovery tower (601) of roots blower (401)；Asphalitine recovery tower
(101) the oil product outlet connection heavy of oil product outlet connection asphalitine pans (205), heavy tar recovery tower (102) is burnt
Oily pans (206), oil product outlet connection tar light oil pans (207) of tar light oil recovery tower (103).
6. coke tar recovery system according to claim 4, which is characterized in that grading stocking system (D) includes mutual
Independent asphalitine storage tank (201), heavy tar storage tank (202), tar light oil storage tank (203) and wastewater storage tank (204)；Drip
The oil outlet of green matter pans (205) connects asphalitine storage tank (201), and the outlet of heavy tar pans (206) oil product is divided into two
Road is connected with heavy tar recovery tower (102) cooling absorbing medium import all the way, another way and grading stocking system
(D) import of heavy tar storage tank (202) is connected in；The outlet of tar light oil pans (207) oil product is divided into two-way, wherein one
The cooling absorbing medium inlet communication on road and tar light oil recovery tower (103), the import of another way and tar light oil storage tank (203)
Connection, tar light oil pans (207) wastewater outlet and wastewater storage tank (204) inlet communication heavy tar pans (206) are useless
Water out is connected with wastewater storage tank (204) import in grading stocking system.
7. coke tar recovery system according to claim 6, which is characterized in that heavy tar recovery tower (102) bottom oil product
Heavy tar pump (301) is provided between outlet and heavy tar pans (206)；Tar light oil recovery tower (103) bottom oil
Tar light oil pump (302) is provided between product outlet and tar light oil pans (207).
8. a kind of tar recovery process, which is characterized in that mixed oil and gas (01) obtains sensible heat asphalitine to be recycled after supercooling
(09) and pitch mixed oil and gas (02) is removed, except pitch mixed oil and gas (02) obtains sensible heat heavy tar (11) to be recycled after cooling
With remove heavy tar mixed oil and gas (03)；
The waste heat of sensible heat asphalitine (09) to be recycled obtains asphalitine (10) after recycling, recycles and stores to asphalitine (10)；
Heavy tar (13), spray heavy tar (14) and oil are obtained after the waste heat of sensible heat heavy tar (11) to be recycled is recovered
Upper waste water (12)；Heavy tar (13) are recycled, waste water (12) carries out waste water recycling device on oil；
Except heavy tar mixed oil and gas (03) obtains sensible heat tar light oil (15) to be recycled and level-one except tar light oil after cooling
Mixed oil and gas (04)；
Sensible heat tar light oil (15) to be recycled waste heat recycling after obtain spray tar light oil (17), the first tar light oil (18) and
Oil is lower waste water (16)；Waste water recycling device is carried out to waste water under oil (16)；First tar light oil (18) is recycled；
Level-one removes tar light oil mixed oil and gas (05) afterwards except tar light oil mixed oil and gas (04) is pressurized for positive pressure level-one, positive pressure one
Grade obtains the second tar light oil (19) and second level except tar light oil mixes after removing the cooling of tar light oil mixed oil and gas (05) depth
Oil gas (06), second level trap to obtain third tar light oil (20) and decoking except tar light oil mixed oil and gas (06) passes through tar droplet
Oil gas (07) carries out recycling storage to the second tar light oil (19) and third tar light oil (20).
9. tar recovery process according to claim 8, which is characterized in that decoking oil gas (07) and mixed oil and gas (01)
Heating decoking oil gas (08) is obtained after carrying out heat exchange；It supplements desalted water (23) and obtains deaerated water (22), deaerated water through deoxygenation
(22) pressurized that successively sensible heat tar light oil (15) to be recycled, sensible heat heavy tar to be recycled (11) and sensible heat to be recycled are dripped
Green matter (09) is cooled down, and respectively corresponds to obtain level-one heat exchange hot water (24), second level heat exchange steam (25) after heat exchange
With three-level heat exchange steam (26), three-level heat exchange steam (26) power required when cooling as the second tar light oil (19).
10. tar recovery process according to claim 8, which is characterized in that three-level heat exchange steam (26) output power
Steam condensate (21) are formed later, steam condensate (21) is successively treated back through being overpressurized after deoxygenation with deaerated water (22) together
Sensible heat tar light oil (15), sensible heat heavy tar to be recycled (11) and sensible heat asphalitine to be recycled (09) is received to be cooled down；
Except pitch mixed oil and gas (02) is cooling using spray heavy tar (14), except heavy tar mixed oil and gas (03) is using spray
Tar light oil (17) is cooling.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112691400A (en) * | 2020-12-30 | 2021-04-23 | 中冶焦耐(大连)工程技术有限公司 | Vacuum system and process for distillation tower for collecting three-mixed fraction vacuum tar |
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