CN109880658B - Tar recovery system and process - Google Patents
Tar recovery system and process Download PDFInfo
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- CN109880658B CN109880658B CN201910270943.9A CN201910270943A CN109880658B CN 109880658 B CN109880658 B CN 109880658B CN 201910270943 A CN201910270943 A CN 201910270943A CN 109880658 B CN109880658 B CN 109880658B
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- 238000011084 recovery Methods 0.000 title claims abstract description 237
- 238000000034 method Methods 0.000 title description 15
- 239000007789 gas Substances 0.000 claims abstract description 119
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000002918 waste heat Substances 0.000 claims abstract description 47
- 239000002826 coolant Substances 0.000 claims abstract description 29
- 239000002351 wastewater Substances 0.000 claims description 55
- 238000001816 cooling Methods 0.000 claims description 26
- 238000005507 spraying Methods 0.000 claims description 23
- 239000012716 precipitator Substances 0.000 claims description 16
- 238000010521 absorption reaction Methods 0.000 claims description 9
- 239000003034 coal gas Substances 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 2
- 230000000153 supplemental effect Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000011269 tar Substances 0.000 description 345
- 239000000047 product Substances 0.000 description 24
- 238000005406 washing Methods 0.000 description 9
- 239000011280 coal tar Substances 0.000 description 6
- 238000000197 pyrolysis Methods 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 238000005411 Van der Waals force Methods 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000000498 cooling water Substances 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
- 238000004508 fractional distillation Methods 0.000 description 1
- 238000001754 furnace pyrolysis Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 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
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Industrial Gases (AREA)
Abstract
The invention discloses a tar recovery system, which comprises a tar grading recovery system A, a light tar deep recovery system B, a waste heat recovery system C and a product grading storage system D; the oil outlet of the tar grading recovery system A is communicated with the oil inlet of the waste heat recovery system C, and the oil outlet of the waste heat recovery system C and the oil outlet of the light tar deep recovery system B are communicated with the product grading storage system D; the waste heat recovery system C is provided with a cooling medium inlet, and a cooling medium outlet of the waste heat recovery system C is communicated with a steam inlet of the light tar deep recovery system B; the gas outlet of the tar grading recovery system A is communicated with the light tar deep recovery system B, and the gas outlet of the light tar deep recovery system B is communicated with the cooling medium inlet of the tar grading recovery system A; solving the problem of difficult separation of tar and water and improving the quality of tar products; the heat energy is effectively recycled, the energy consumption of the system is effectively reduced, the water consumption of the system is extremely low, and the water-saving effect is obvious.
Description
Technical Field
The invention belongs to the technical field of coal chemical industry, and particularly relates to a tar recovery system and a tar recovery process.
Background
Coal tar is used as a main high added value product of a coal pyrolysis technology, and the yield and the quality of the coal tar are main factors influencing the economy of the coal pyrolysis technology. The recovery mode of coal tar mainly comprises dry recovery and wet recovery. At present, a wet method is adopted in relatively mature and high industrialization degree, and a water washing method using water (ammonia water) as a detergent is mainly adopted in the vertical furnace pyrolysis technology. The water washing tower mainly comprises a spray tower, a Venturi tower, an impact bubbling washing tower, a packed tower and the like. The essence of water washing is cooling effect, has good removal effect on heavy tar, but has lower operation temperature, and can generate sticky particles and salts to cause coking, and block pipelines and valves. The strong polarity of water can realize the dissolution and elution of heterocyclic atom tar, but the coke-washing wastewater becomes complex phenol-containing suspension, and the treatment cost is extremely high; the strong polarity of water has no affinity for hydrocarbon tars and thus has poor removal, which in fact controls the dew point of the tar in the pyrolysis gas. Therefore, the water washing method cannot achieve a satisfactory tar recovery effect from the viewpoint of purification degree and environmental protection.
The oil-based tar recovery method utilizes the compatibility of the cooling oil absorbent and tar, namely the Van der Waals force effect, so that the method has the advantages of washing oil, avoiding the pollution problem of phenolic wastewater, improving the removal effect of light hydrocarbon tar, and reducing the dew point of coal gas tar below the operating temperature due to the absorption effect. However, the corresponding problems of the current oil washing process are not solved. Firstly, the existing oil washing method is generally a two-to-three-stage cooling process, the first-stage cooling oil is circulated at a temperature higher than 200 ℃, and the coal tar is easy to react for the second time to form coking under the condition of higher temperature, so that the quality and yield of the tar are affected; secondly, the density of the coal tar which is mixed and collected is about 1.05 and is close to that of water, so that oil-water separation is difficult to realize, and the subsequent use of the coal tar is not facilitated; thirdly, the temperature of the cooling tail end is controlled to be about 50 ℃ mostly, most tar recovery is operated under the micro negative pressure condition, and is limited by gas-liquid balance, a large amount of light components still cannot be recovered, and the stable operation of downstream equipment and the further use of coal gas are affected; fourth, the system uses a large amount of circulating cooling water and the heat is not utilized effectively.
Disclosure of Invention
In order to solve the problems in the prior art, the invention discloses a low-energy-consumption high-yield tar recovery system and a low-energy-consumption high-yield tar recovery process for solving the problems of low tar recovery rate, large system cold consumption, unutilized tar sensible heat and the like of the existing tar recovery system.
In order to achieve the aim, the invention adopts the technical scheme that the tar recovery system comprises a tar grading recovery system, a light tar deep recovery system, a waste heat recovery system and a product grading storage system; the oil outlet of the tar grading recovery system is communicated with the oil inlet of the waste heat recovery system, and the oil outlet of the waste heat recovery system and the oil outlet of the light tar deep recovery system are communicated with the product grading storage system; the waste heat recovery system is provided with a cooling medium inlet, and a cooling medium outlet of the waste heat recovery system is communicated with a steam inlet of the light tar deep recovery system; the gas outlet of the tar grading recovery system is communicated with the light tar deep recovery system, and the gas outlet of the light tar deep recovery system is communicated with the cooling medium inlet of the tar grading recovery system.
The tar grading recovery system comprises an asphaltene recovery tower, a heavy tar recovery tower and a light tar recovery tower, wherein a gas outlet at the top of the asphaltene recovery tower is connected with a heavy tar recovery tower inlet, and a gas outlet at the top of the heavy tar recovery tower is connected with a light tar recovery tower inlet; the outlet of the light tar recovery tower is connected with a light tar deep recovery system; and outlets of the asphaltene recovery tower, the heavy tar recovery tower and the light tar recovery tower are all connected with a waste heat recovery system.
The light tar deep recovery system comprises a low-temperature recovery tower and an electric tar precipitator, wherein a gas outlet of the low-temperature recovery tower is connected with the electric tar precipitator, and oil outlets of the low-temperature recovery tower and the electric tar precipitator are both connected with a product classification storage system; the top of the electric tar precipitator is provided with a gas outlet which is communicated with a cooling medium inlet of the tar grading recovery system.
The waste heat recovery system comprises a deaerator, a light tar intermediate tank, a heavy tar intermediate tank and an asphaltene intermediate tank which are sequentially communicated along the flow direction of a cooling medium; the cooling medium outlet of the asphaltene intermediate tank is communicated with the steam inlet of the low-temperature recovery tower; the low-temperature recovery tower steam condensate outlet is communicated with a deaerator; a water supply pump is arranged on a pipeline for communicating the deaerator with the light tar intermediate tank.
The outlet of the light tar recovery tower is connected with the Roots blower, and the outlet of the Roots blower is connected with the inlet of the low-temperature recovery tower; the oil outlet of the asphaltene recovery tower is connected with the asphaltene intermediate tank, the oil outlet of the heavy tar recovery tower is connected with the heavy tar intermediate tank, and the oil outlet of the light tar recovery tower is connected with the light tar intermediate tank.
The product classification storage system comprises an asphaltene storage tank, a heavy tar storage tank, a light tar storage tank and a wastewater storage tank which are mutually independent; an oil outlet of the asphaltene intermediate tank is connected with an asphaltene storage tank, an oil outlet of the heavy tar intermediate tank is divided into two paths, one path is connected with a cooling absorption medium inlet of a heavy tar recovery tower, and the other path is connected with an inlet of a heavy tar storage tank in a product classification storage system; the oil product outlet of the light tar intermediate tank is divided into two paths, wherein one path is communicated with the cooling absorption medium inlet of the light tar recovery tower, the other path is communicated with the inlet of the light tar storage tank, the waste water outlet of the light tar intermediate tank is communicated with the inlet of the waste water storage tank, and the waste water outlet of the heavy tar intermediate tank is connected with the inlet of the waste water storage tank in the product classification storage system.
A heavy tar pump is arranged between the oil outlet at the bottom of the heavy tar recovery tower and the heavy tar intermediate tank; a light tar pump is arranged between the oil outlet at the bottom of the light tar recovery tower and the light tar intermediate tank.
The mixed oil gas is cooled to obtain sensible heat asphaltene to be recovered and deasphalted mixed oil gas, and the deasphalted mixed oil gas is cooled to obtain sensible heat heavy tar to be recovered and deasphalted mixed oil gas;
recovering the waste heat of the sensible heat asphaltene to obtain asphaltene, and recovering and storing the asphaltene;
recovering the waste heat of the sensible heat heavy tar to obtain heavy tar, spraying the heavy tar and oily wastewater; recycling heavy tar and wastewater on oil to perform wastewater recycling treatment;
cooling the heavy tar removed mixed oil gas to obtain sensible heat light tar to be recovered and primary light tar removed mixed oil gas;
After the waste heat of the sensible heat light tar is recovered, spraying light tar, first light tar and wastewater under oil are obtained; carrying out wastewater recovery treatment on the wastewater under oil; recovering the first light tar;
The first-stage light tar removal mixed oil gas is pressurized to be positive-pressure first-stage light tar removal mixed oil gas, the positive-pressure first-stage light tar removal mixed oil gas is deeply cooled to obtain second light tar and second-stage light tar removal mixed oil gas, the second-stage light tar removal mixed oil gas is trapped by tar droplets to obtain third light tar and tar removal coal gas, and the second light tar and the third light tar are recycled and stored.
The tar-removed gas and the mixed oil gas are subjected to heat exchange to obtain the heating tar-removed gas; the supplementary desalted water is deoxidized to obtain deoxidized water, the deoxidized water is pressurized to cool the sensible heat light tar to be recovered, the sensible heat heavy tar to be recovered and the sensible heat asphaltene to be recovered in sequence, and after heat exchange, primary heat exchange hot water, secondary heat exchange steam and tertiary heat exchange steam are respectively and correspondingly obtained, wherein the tertiary heat exchange steam is used as power required by cooling the second light tar.
The three-stage heat exchange steam outputs power to form steam condensate, and the steam condensate is deoxygenated and then pressurized together with deoxygenated water to sequentially cool sensible heat light tar to be recovered, sensible heat heavy tar to be recovered and sensible heat asphaltene to be recovered;
the mixed oil gas for removing asphalt is cooled by spraying heavy tar, and the mixed oil gas for removing heavy tar is cooled by spraying light tar.
Compared with the prior art, the invention has at least the following beneficial effects:
1. The tar product has high yield and good quality: compared with the traditional technology, the technical scheme of the invention has the advantages that the light tar recovery section is added, the product yield is effectively improved, meanwhile, the problem of difficult separation of tar and water can be effectively avoided by the fractional distillation and sectional product recovery mode, and the quality of tar products is ensured;
2. The product recovered by the recovery system and the process of the invention is convenient for downstream connection, and the industrial chain is prolonged: the method has the advantages that the boiling point cutting flow of the subsequent tar processing can be simplified for asphaltene, heavy tar and light tar products respectively stored after the tar is recovered, the residual amount of tar in pyrolysis gas passing through a light tar recovery system is greatly reduced for pyrolysis gas, and the further utilization of the pyrolysis gas is facilitated;
3. The heat energy is effectively recycled, the energy consumption of the system is effectively reduced, a large amount of sensible heat byproduct steam of the high-temperature mixed oil gas is effectively recovered through gradual utilization of the energy, and low-temperature power is provided by utilizing the byproduct steam, so that the energy consumption and other power consumption required for effectively recovering light components are obviously reduced;
4. The system has extremely low water consumption and obvious water-saving effect: the deoxygenated water is subjected to tar heat byproduct steam recovery in the process, and the byproduct steam is condensed in the low-temperature recovery device to form steam condensate which is further returned to the deoxygenator to be used as a cooling medium, so that closed cycle of public engineering water can be formed only by supplementing a very small amount of desalted water outside, a great deal of loss of circulating water is avoided, the water consumption of a system is reduced, the investment of a cooling tower or air cooling is avoided, and the contradiction that common coal resources are rich in regions, water resources are relatively scarce and the loss of the circulating water is relatively large is also relieved.
Drawings
FIG. 1 is a schematic illustration of the process flow of the present invention;
FIG. 2 is a schematic diagram of a tar recovery process system of the present invention;
In the drawing, the A-tar grading recovery system B-light tar deep recovery system C-waste heat recovery system D-product grading storage system;
101-asphaltene recovery tower, 102-heavy tar recovery tower, 103-light tar recovery tower, 401-Roots blower, 601-low temperature recovery tower, 501-electrical tar precipitator, 201-asphaltene storage tank, 202-heavy tar storage tank, 203-light tar storage tank, 204-wastewater storage tank, 205-asphaltene intermediate tank 206-heavy tar intermediate tank 207-light tar intermediate tank, 208-deaerator, 301-heavy tar pump, 302-light tar pump, 303-water feed pump, 01-high temperature mixed oil and gas, 02-deasphalted mixed oil and gas, 03-deasphalted mixed oil and gas, 04-first stage deasphalted mixed oil and gas, 05-positive pressure first stage deasphalted mixed oil and gas, 06-second stage deasphalted mixed oil and gas, 07-deasphalted gas, 08-high temperature deasphalted gas, 09-sensible heat asphaltene to be recovered, 10-asphaltene, 11-sensible heat heavy tar to be recovered, 12-upper wastewater, 13-heavy tar to be recovered, 14-sensible heat light tar to be recovered, 16-lower-oil, 17-spray light tar, 18-first stage, 19-first stage deasphalted water, 19-second stage deasphalted water, 19-third stage, 25-heat exchange water, and third stage, and fourth stage, and heat exchange water vapor, and heat exchange.
Detailed Description
The invention is described in detail below with reference to specific embodiments and the accompanying drawings.
A tar recovery system comprises a tar grading recovery system A, a light tar deep recovery system B, a waste heat recovery system C and a product grading storage system D; the oil outlet of the tar grading recovery system A is communicated with the oil inlet of the waste heat recovery system C, and the oil outlet of the waste heat recovery system C and the oil outlet of the light tar deep recovery system B are communicated with the product grading storage system D; the waste heat recovery system C is provided with a cooling medium inlet, and a cooling medium outlet of the waste heat recovery system C is communicated with a steam inlet of the light tar deep recovery system B; the gas outlet of the tar grading recovery system A is communicated with the light tar deep recovery system B, and the gas outlet of the light tar deep recovery system B is communicated with the cooling medium inlet of the tar grading recovery system A.
Wherein the tar classification recovery system comprises an asphaltene recovery tower 101, a heavy tar recovery tower 102 and a light tar recovery tower 103; the top gas outlet of the asphaltene recovery tower 101 is connected with the inlet of the heavy tar recovery tower 102, and the top gas outlet of the heavy tar recovery tower 102 is connected with the inlet of the light tar recovery tower 103;
the light tar deep recovery system comprises a Roots blower 401, a low-temperature recovery tower 601 and an electric tar precipitator 501; the outlet of the Roots blower 401 is connected with the inlet of the low-temperature recovery tower 601, and the gas outlet of the low-temperature recovery tower 601 is connected with the inlet of the electric tar precipitator 501;
The waste heat recovery system comprises a deaerator 208, a feed pump 303, a light tar intermediate tank 207, a heavy tar intermediate tank 206 and an asphaltene intermediate tank 205; the deoxygenated water outlet of the deoxygenator 208 is connected with the inlet of the water feed pump 303, the outlet of the water feed pump 303 is connected with the cooling medium inlet of the light tar intermediate tank 207, the cooling medium outlet of the light tar intermediate tank 207 is connected with the cooling medium inlet of the heavy tar intermediate tank 206, and the cooling medium outlet of the heavy tar intermediate tank 206 is connected with the cooling medium inlet of the asphaltene intermediate tank 205; the outlet of the heavy tar pump 301 is connected with the oil inlet of the heavy tar intermediate tank 206, and the outlet of the light tar pump 302 is connected with the oil inlet of the light tar intermediate tank 207.
The product staging storage system includes an asphaltene storage tank 201, a heavy tar storage tank 202, a light tar storage tank 203, and a wastewater storage tank 204.
The bottom oil outlet of the asphaltene recovery tower 101 in the tar classification recovery system is connected with the oil inlet of the asphaltene middle tank 205 in the waste heat recovery system, the bottom oil outlet of the heavy tar recovery tower 102 is connected with the inlet of the heavy tar pump 301 in the waste heat recovery system C, the bottom oil outlet of the light tar recovery tower 103 is connected with the inlet of the light tar pump 302 in the waste heat recovery system C, and the gas outlet at the top of the light tar recovery tower 103 is connected with the inlet of the Roots blower 401 in the light tar deep recovery system B.
The oil outlet of the low-temperature recovery tower 601 in the light tar deep recovery system and the oil outlet of the electric tar precipitator 501 are connected with the inlet of the light tar storage tank 203 in the product classification storage system; the gas outlet of the electric tar precipitator 501 is connected with the cooling medium inlet of the asphaltene recovery tower 101 in the tar grading recovery system, and the steam condensate outlet of the low-temperature recovery tower 601 is connected with the inlet of the deaerator 208 in the waste heat recovery system.
The oil outlet of the heavy tar intermediate tank 206 in the waste heat recovery system is divided into two paths, one path is connected with the cooling absorption medium inlet of the heavy tar recovery tower 102 in the tar grading recovery system, the other path is connected with the inlet of the heavy tar storage tank 202 in the product grading storage system, and the waste water outlet of the heavy tar intermediate tank 206 is connected with the inlet of the waste water storage tank 204 in the product grading storage system; the oil outlet of the light tar intermediate tank 207 is divided into two paths, one path is connected with the cooling absorption medium inlet of the light tar recovery tower 103 in the tar grading recovery system, the other path is connected with the light tar storage tank 203 inlet in the product grading storage system, and the waste water outlet of the light tar intermediate tank 207 is connected with the waste water storage tank 204 inlet in the product grading storage system; the cooling medium outlet of the asphaltene intermediate tank 205 is connected with the steam inlet of the low-temperature recovery tower 601 in the light tar deep recovery system, and the oil outlet of the asphaltene intermediate tank 205 is connected with the inlet of the asphaltene storage tank 201 in the product classification storage system.
The high-temperature mixed oil gas 01 with the temperature of 450-700 ℃ enters an asphaltene recovery tower 101, the sensible heat asphaltene 09 to be recovered with the temperature of 300-360 ℃ and the deasphalting mixed oil gas 02 with the temperature of 300-360 ℃ are obtained after cooling, the sensible heat asphaltene 09 to be recovered enters an asphaltene middle tank 205, the asphaltene enters a heavy tar recovery tower 102, the sensible heat heavy tar 11 to be recovered with the temperature of 170-210 ℃ and the deasphalting mixed oil gas 03 with the temperature of 170-210 ℃ are obtained after cooling by spraying the heavy tar 14, the sensible heat heavy tar 11 to be recovered enters a heavy tar middle tank 206 by a heavy tar pump 301, the deasphalting mixed oil gas 03 enters a light tar recovery tower 103, The sensible heat light tar 15 to be recovered and the first-stage light tar removal mixed oil gas 04 with the temperature of 50-80 ℃ are obtained after being cooled by spraying the light tar 17, the sensible heat light tar 15 to be recovered enters a light tar intermediate tank 207 through a light tar pump 302, the first-stage light tar removal mixed oil gas 04 is pressurized into a positive pressure first-stage light tar removal mixed oil gas 05 through a Roots blower 401, the pressure is 8-15 kPa, the positive pressure first-stage light tar removal mixed oil gas 05 is deeply cooled to the temperature of 10-25 ℃ through a low temperature recovery tower 601 to obtain light tar 19 and a second-stage light tar removal mixed oil gas 06, the second-stage light tar removal mixed oil gas 06 is electrically treated by a tar precipitator 501 to obtain light tar 20 and tar removal gas 07, The tar-removed gas 07 enters an asphaltene recovery tower 101 as a cooling medium, and high-temperature tar-removed gas 08 is obtained after heat exchange; The steam condensate 21 and the supplementary desalted water 23 of the low-temperature recovery tower 601 are subjected to deaeration by a deaerator 208, deoxidized water 22 sequentially passes through a light tar intermediate tank 207, a heavy tar intermediate tank 206 and an asphaltene intermediate tank 205 by a water feeding pump 303, and is subjected to heat exchange to respectively obtain primary heat exchange hot water 24, secondary heat exchange steam 25 and tertiary heat exchange steam 26, wherein the tertiary heat exchange steam 26 enters the low-temperature recovery tower 601 to provide a low-temperature environment of 8-15 ℃; the sensible heat to be recovered asphaltenes 09 are subjected to waste heat recovery in an asphaltene intermediate tank 205 to obtain asphaltenes 10, and the asphaltenes 10 enter an asphaltene storage tank 201; After the sensible heat heavy tar 11 to be recovered is subjected to waste heat recovery in a heavy tar intermediate tank 206, obtaining heavy tar 13, spraying the heavy tar 14 and oily wastewater 12, wherein the heavy tar 13 enters a heavy tar storage tank 202, spraying the heavy tar 14 into a heavy tar recovery tower 102, and the oily wastewater 12 enters a wastewater storage tank 204; after the sensible heat light tar 15 to be recovered is subjected to waste heat recovery in a light tar storage tank 207, spraying light tar 17, first light tar 18 and oily wastewater 16 are obtained, the oily wastewater 16 enters a wastewater storage tank 204, the spraying light tar 17 enters a light tar recovery tower 103, and the first light tar 18, the second light tar 19 and the third light tar 20 enter a light tar storage tank 203 together; The first light tar 18, the second light tar 19, and the third light tar 20 of the present invention are essentially the same, "first," "second," and "third" are merely intended to aid in understanding the process and system of the present invention.
Examples:
Example 1:
The high-temperature mixed oil gas 01 with parameters of 550 ℃ and 3KPa enters an asphaltene recovery tower 101, after cooling, sensible heat asphaltene 09 to be recovered at about 360 ℃ and deasphalted mixed oil gas 02 at about 360 ℃ are obtained, sensible heat asphaltene 09 to be recovered enters an asphaltene middle tank 205, 1KPa deasphalted mixed oil gas 02 enters a heavy tar recovery tower 102, after spraying heavy tar 14 and cooling, sensible heat heavy tar 11 to be recovered at about 210 ℃ and heavy tar removed mixed oil gas 03 at about 210 ℃ are obtained, sensible heat heavy tar 11 to be recovered enters a heavy tar middle tank 206 through a heavy tar pump 301, 5KPa deasphalted mixed oil gas 03 enters a light tar recovery tower 103, after spraying light tar 17 and cooling, sensible heat light tar 15 to be recovered at about 50 ℃ and first-grade deasphalted mixed oil gas 04 are obtained, the sensible heat light tar 15 to be recovered enters a light tar intermediate tank 207 through a light tar pump 302, the first-stage light tar removal mixed oil gas 04 is pressurized into positive pressure first-stage light tar removal mixed oil gas 05 through a Roots blower 401, the pressure is about 10kPa, the positive pressure first-stage light tar removal mixed oil gas 05 is deeply cooled to 8-15 ℃ through a low-temperature recovery tower 601 to obtain light tar 19 and second-stage light tar removal mixed oil gas 06, the second-stage light tar removal mixed oil gas 06 is subjected to electric tar precipitator 501 to obtain light tar 20 and tar removal gas 07, the tar removal gas 07 enters an asphaltene recovery tower 101 to serve as a cooling medium, and a high-temperature tar removal gas 08 output boundary zone is obtained after heat exchange; the steam condensate 21 and the supplementary desalted water 23 of the low-temperature recovery tower 601 pass through a deaerator 208 to obtain deoxidized water 22, the deoxidized water 22 passes through a light tar intermediate tank 207, a heavy tar intermediate tank 206 and an asphaltene intermediate tank 205 in sequence through a water feeding pump 303, after heat exchange, primary heat exchange hot water 24, secondary heat exchange steam 25 and tertiary heat exchange steam 26 are respectively obtained, and medium-pressure three-stage heat exchange steam 26 with the pressure of 3.5MPa enters the steam jet type low-temperature recovery tower 601 to provide a low-temperature environment of 8-15 ℃, wherein the medium-pressure heat exchange steam is steam with the pressure of 2.5-6 MPa only; the sensible heat to be recovered asphaltene 09 is subjected to waste heat recovery in an asphaltene intermediate tank 205 to obtain asphaltene 10, the asphaltene 10 enters an asphaltene storage tank 201, the sensible heat to be recovered heavy tar 11 is subjected to waste heat recovery in a heavy tar intermediate tank 206 to obtain heavy tar 13, sprayed heavy tar 14 and oily wastewater 12, the heavy tar 13 enters a heavy tar storage tank 202, sprayed heavy tar 14 enters a heavy tar recovery tower 102, and oily wastewater 12 enters a wastewater storage tank 204; after the sensible heat light tar 15 to be recovered is subjected to waste heat recovery in the light tar storage tank 207, sprayed light tar 17, first light tar 18 and oily wastewater 16 are obtained, the oily wastewater 16 enters the wastewater storage tank 204, the sprayed light tar 17 enters the light tar recovery tower 103, and the first light tar 18, the second light tar 19 and the third light tar 20 enter the light tar storage tank 203 together.
Example 2
The high-temperature mixed oil gas 01 with parameters of 450-700 ℃ and 3KPa enters an asphaltene recovery tower 101, the sensible heat asphaltene 09 to be recovered and the deasphalted mixed oil gas 02 with the temperature of about 360 ℃ are obtained after deoxidized water cooling, medium-high pressure steam is produced as a byproduct, the sensible heat asphaltene 09 to be recovered enters an asphaltene intermediate tank 205, the deasphalted mixed oil gas 02 with the temperature of-1 KPa enters a heavy tar recovery tower 102, the sensible heat heavy tar 11 to be recovered and the deasphalted mixed oil gas 03 with the temperature of about 210 ℃ are obtained after spraying heavy tar 14 for cooling, the sensible heat heavy tar 11 to be recovered enters a heavy tar intermediate tank 206 with a heavy tar pump 301, the deasphalted mixed oil gas 03 with the temperature of-5 KPa enters a light tar recovery tower 103, the sensible heat light tar 15 to be recovered and the first-stage light tar removal mixed oil gas 04 at the temperature of about 50 ℃ are obtained after the sprayed light tar 17 is cooled, the sensible heat light tar 15 to be recovered enters a light tar intermediate tank 207 through a light tar pump 302, the first-stage light tar removal mixed oil gas 04 is pressurized into a positive pressure first-stage light tar removal mixed oil gas 05 through a Roots blower 401, the pressure is about 10kPa, the positive pressure first-stage light tar removal mixed oil gas 05 is deeply cooled to 8-15 ℃ through a low-temperature recovery tower 601 to obtain light tar 19 and a second-stage light tar removal mixed oil gas 06, the second-stage light tar removal mixed oil gas 06 is subjected to electric tar precipitator 501 to obtain light tar 20 and tar removal gas 07, and the tar removal gas 07 is taken as a product output boundary zone; the steam condensate 21 and the supplementary desalted water 23 of the low-temperature recovery tower 601 pass through a deaerator 208 to obtain deoxidized water 22, the deoxidized water 22 is divided into two paths by a water feeding pump 303, one path of deoxidized water passes through a light tar intermediate tank 207 and a heavy tar intermediate tank 206 in sequence to obtain secondary heat exchange steam 25, and the secondary heat exchange steam 25 enters the deaerator 208 to be used as power of the deaerator 208; the other way of deoxygenated water 22 enters an asphaltene middle tank 205 for heat exchange, medium-pressure steam obtained through heat exchange enters a steam absorption type low-temperature recovery tower 601 to provide a low-temperature environment of 8-15 ℃, and cooled asphaltene enters the asphaltene storage tank 201 after being further cooled by an external oil-throwing cooler; after the sensible heat heavy tar 11 to be recovered is subjected to waste heat recovery in a heavy tar intermediate tank 206, obtaining heavy tar 13, spraying the heavy tar 14 and oily wastewater 12, wherein the heavy tar 13 enters a heavy tar storage tank 202, spraying the heavy tar 14 into a heavy tar recovery tower 102, and the oily wastewater 12 enters a wastewater storage tank 204; after the sensible heat light tar 15 to be recovered is subjected to waste heat recovery in the light tar storage tank 207, sprayed light tar 17, first light tar 18 and oily wastewater 16 are obtained, the oily wastewater 16 enters the wastewater storage tank 204, the sprayed light tar 17 enters the light tar recovery tower 103, and the first light tar 18, the second light tar 19 and the third light tar 20 enter the light tar storage tank 203 together.
Example 3:
the high-temperature mixed oil gas 01 with the parameters of 450-700 ℃ and 3KPa enters an asphaltene recovery tower 101, and after tar-removed coal gas 07 is cooled, the sensible heat asphaltene 09 to be recovered at the temperature of about 360 ℃ and the deasphalted mixed oil gas 02 at the temperature of about 360 ℃ are obtained, and the sensible heat asphaltene 09 to be recovered enters an asphalt intermediate tank 205; the method comprises the steps that-1 KPa deasphalting mixed oil gas 02 enters a heavy tar recovery tower 102, sensible heat 11 to be recovered and heavy tar removing mixed oil gas 03 at the temperature of about 210 ℃ are obtained after cooling by spraying heavy tar 14, the sensible heat 11 to be recovered enters a heavy tar middle tank 206 through a heavy tar pump 301, 5KPa deasphalting mixed oil gas 03 enters a light tar recovery tower 103, sensible heat 15 to be recovered and primary deasphalting mixed oil gas 04 at the temperature of about 50 ℃ are obtained after cooling by spraying light tar 17, the sensible heat 15 to be recovered enters a light tar middle tank 207 through a light tar pump 302, the primary deasphalting mixed oil gas 04 is pressurized into positive pressure primary deasphalting mixed oil gas 05 through a Roots blower 401, the pressure is about 10kPa, the positive pressure primary deasphalting mixed oil gas 05 is deeply cooled to 8-15 ℃ through a low temperature recovery tower 601 to obtain light tar 19 and secondary deasphalting mixed oil gas 06, the secondary deasphalting mixed oil gas 06 is obtained through an electrical tar absorber 501, the light tar 15 and the deasphalting gas 07 enters the asphaltene recovery tower 101 to be used as a cooling medium, and the high temperature gas 08 is output in a high temperature range; the steam condensate 21 and the supplementary desalted water 23 of the low-temperature recovery tower 601 pass through a deaerator 208 to obtain deoxidized water 22, the deoxidized water 22 is divided into two paths by a water feeding pump 303, one path of deoxidized water passes through a light tar intermediate tank 207 and a heavy tar intermediate tank 206 in sequence to obtain secondary heat exchange steam 25, and the secondary heat exchange steam 25 enters the deaerator 208 to be used as power of the deaerator 208; the other way of deoxygenated water 22 enters an asphaltene middle tank 205 for heat exchange, medium-pressure steam obtained through heat exchange enters a steam absorption type low-temperature recovery tower 601 to provide a low-temperature environment of 8-15 ℃, and cooled asphaltene enters the asphaltene storage tank 201 after being further cooled by an external oil-throwing cooler; after the sensible heat heavy tar 11 to be recovered is subjected to waste heat recovery in a heavy tar intermediate tank 206, obtaining heavy tar 13, spraying the heavy tar 14 and oily wastewater 12, wherein the heavy tar 13 enters a heavy tar storage tank 202, spraying the heavy tar 14 into a heavy tar recovery tower 102, and the oily wastewater 12 enters a wastewater storage tank 204; after the sensible heat light tar 15 to be recovered is subjected to waste heat recovery in the light tar storage tank 207, sprayed light tar 17, first light tar 18 and oily wastewater 16 are obtained, the oily wastewater 16 enters the wastewater storage tank 204, the sprayed light tar 17 enters the light tar recovery tower 103, and the first light tar 18, the second light tar 19 and the third light tar 20 enter the light tar storage tank 203 together.
Claims (5)
1. The tar recovery system is characterized by comprising a tar grading recovery system (A), a light tar deep recovery system (B), a waste heat recovery system (C) and a product grading storage system (D); the oil outlet of the tar grading recovery system (A) is communicated with the oil inlet of the waste heat recovery system (C), and the oil outlet of the waste heat recovery system (C) and the oil outlet of the light tar deep recovery system (B) are communicated with the product grading storage system (D); the waste heat recovery system (C) is provided with a cooling medium inlet, and a cooling medium outlet of the waste heat recovery system (C) is communicated with a steam inlet of the light tar deep recovery system (B); the gas outlet of the tar grading recovery system (A) is communicated with the light tar deep recovery system (B), and the gas outlet of the light tar deep recovery system (B) is communicated with the cooling medium inlet of the tar grading recovery system (A);
The tar classification recovery system (A) comprises an asphaltene recovery tower (101), a heavy tar recovery tower (102) and a light tar recovery tower (103), wherein a gas outlet at the top of the asphaltene recovery tower (101) is connected with an inlet of the heavy tar recovery tower (102), and a gas outlet at the top of the heavy tar recovery tower (102) is connected with an inlet of the light tar recovery tower (103); an outlet of the light tar recovery tower (103) is connected with a light tar deep recovery system (B); outlets of the asphaltene recovery tower (101), the heavy tar recovery tower (102) and the light tar recovery tower (103) are all connected with a waste heat recovery system (C); the light tar deep recovery system (B) comprises a low-temperature recovery tower (601) and an electric tar precipitator (501), a gas outlet of the low-temperature recovery tower (601) is connected with the electric tar precipitator (501), and oil outlets of the low-temperature recovery tower (601) and the electric tar precipitator (501) are both connected with a product classification storage system (D); the top of the electric tar precipitator (501) is provided with a gas outlet which is communicated with a cooling medium inlet of the tar grading recovery system (A);
The waste heat recovery system (C) comprises a deaerator (208), a light tar intermediate tank (207), a heavy tar intermediate tank (206) and an asphaltene intermediate tank (205) which are sequentially communicated along the flow direction of a cooling medium; the cooling medium outlet of the asphaltene intermediate tank (205) is communicated with the steam inlet of the low-temperature recovery tower (601); the steam condensate outlet of the low-temperature recovery tower (601) is communicated with the deaerator (208); a water supply pump (303) is arranged on a pipeline of the deaerator (208) communicated with the light tar intermediate tank (207);
The outlet of the light tar recovery tower (103) is connected with a Roots blower (401), and the outlet of the Roots blower (401) is connected with the inlet of the low-temperature recovery tower (601);
The product classification storage system (D) is internally provided with a waste water storage tank (204), a waste water outlet of the light tar intermediate tank (207) is communicated with an inlet of the waste water storage tank (204), and a waste water outlet of the heavy tar intermediate tank (206) is connected with an inlet of the waste water storage tank (204) in the product classification storage system.
2. The tar recovery system according to claim 1, wherein an oil outlet of the asphaltene recovery tower (101) is connected to the asphaltene intermediate tank (205), an oil outlet of the heavy tar recovery tower (102) is connected to the heavy tar intermediate tank (206), and an oil outlet of the light tar recovery tower (103) is connected to the light tar intermediate tank (207).
3. The tar recovery system according to claim 1, wherein the product staging storage system (D) comprises an asphaltene storage tank (201), a heavy tar storage tank (202) and a light tar storage tank (203) that are independent of each other; an oil outlet of the asphaltene intermediate tank (205) is connected with the asphaltene storage tank (201), an oil outlet of the heavy tar intermediate tank (206) is divided into two paths, one path is connected with a cooling absorption medium inlet of the heavy tar recovery tower (102), and the other path is connected with an inlet of the heavy tar storage tank (202) in the product classification storage system (D); the oil outlet of the light tar intermediate tank (207) is divided into two paths, wherein one path is communicated with the cooling absorption medium inlet of the light tar recovery tower (103), and the other path is communicated with the inlet of the light tar storage tank (203).
4. A tar recovery system according to claim 3, characterized in that a heavy tar pump (301) is arranged between the bottom oil outlet of the heavy tar recovery tower (102) and the heavy tar intermediate tank (206); a light tar pump (302) is arranged between the oil outlet at the bottom of the light tar recovery tower (103) and the light tar intermediate tank (207).
5. A tar recovery process, characterized in that based on the tar recovery system of any one of claims 1-4, the mixed oil gas (01) is cooled to obtain sensible heat asphaltene (09) to be recovered and deasphalted mixed oil gas (02), and the deasphalted mixed oil gas (02) is cooled to obtain sensible heat heavy tar (11) to be recovered and deasphalted mixed oil gas (03);
recovering the waste heat of the sensible heat asphaltene (09) to obtain asphaltene (10), and recovering and storing the asphaltene (10);
Recovering the waste heat of the sensible heat heavy tar (11) to obtain heavy tar (13), spraying the heavy tar (14) and oily wastewater (12); recovering heavy tar (13), and carrying out wastewater recovery treatment on oily wastewater (12);
Cooling the heavy tar removal mixed oil gas (03) to obtain sensible heat light tar (15) to be recovered and primary light tar removal mixed oil gas (04);
After the waste heat of the sensible heat light tar (15) is recovered, spraying light tar (17), first light tar (18) and oily wastewater (16) are obtained; waste water recovery treatment is carried out on the wastewater (16) under oil; recovering the first light tar (18);
The first-stage light tar removal mixed oil gas (04) is pressurized to be positive-pressure first-stage light tar removal mixed oil gas (05), the positive-pressure first-stage light tar removal mixed oil gas (05) is deeply cooled to obtain second light tar (19) and second-stage light tar removal mixed oil gas (06), the second-stage light tar removal mixed oil gas (06) is trapped by tar droplets to obtain third light tar (20) and tar removal coal gas (07), and the second light tar (19) and the third light tar (20) are recycled and stored; the tar-removed gas (07) and the mixed oil gas (01) are subjected to heat exchange to obtain heating tar-removed gas (08); the supplemental desalted water (23) is deoxidized to obtain deoxidized water (22), the deoxidized water (22) is pressurized to cool the sensible heat light tar (15) to be recovered, the sensible heat heavy tar (11) to be recovered and the sensible heat asphaltene (09) to be recovered in sequence, after heat exchange, primary heat exchange hot water (24), secondary heat exchange steam (25) and tertiary heat exchange steam (26) are respectively correspondingly obtained, and the tertiary heat exchange steam (26) is used as power required by cooling the second light tar (19); the three-stage heat exchange steam (26) outputs power to form steam condensate (21), and the steam condensate (21) is deoxygenated and then pressurized together with deoxygenated water (22) to sequentially cool sensible heat light tar (15) to be recovered, sensible heat heavy tar (11) to be recovered and sensible heat asphaltene (09) to be recovered;
The asphalt-removing mixed oil gas (02) is cooled by spraying heavy tar (14), and the heavy tar-removing mixed oil gas (03) is cooled by spraying light tar (17).
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| CN209722064U (en) * | 2019-04-04 | 2019-12-03 | 陕西煤业化工技术研究院有限责任公司 | A kind of coke tar recovery system |
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| CN103194274B (en) * | 2013-04-16 | 2014-06-04 | 中冶焦耐工程技术有限公司 | A coke oven gas waste heat recovery method and device |
| CN105779028B (en) * | 2016-04-07 | 2019-04-19 | 青岛科大隆腾科技发展有限公司 | Raw coke oven gas heat and change based on washing rectifying produce the method recycled simultaneously |
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| CN103965971A (en) * | 2014-05-20 | 2014-08-06 | 湖南华银能源技术有限公司 | Twin tower coal tar recycling system and twin tower coal tar recycling method |
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