CN105331384A - Modified asphalt continuous production system and method - Google Patents
Modified asphalt continuous production system and method Download PDFInfo
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- CN105331384A CN105331384A CN201510821127.4A CN201510821127A CN105331384A CN 105331384 A CN105331384 A CN 105331384A CN 201510821127 A CN201510821127 A CN 201510821127A CN 105331384 A CN105331384 A CN 105331384A
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Abstract
The invention discloses a modified asphalt continuous production system and method. The system comprises a second evaporator, a first reaction kettle, a second reaction kettle and an asphalt overhead tank, wherein the second evaporator is connected with the bottom of the first reaction kettle through a bridging pipeline, the first reaction kettle is connected with the bottom of the second reaction kettle through an overflow pipe, and the second reaction kettle is connected with the asphalt overhead tank through a finished product pipe. According to the method, mid-temperature asphalt discharged from the bottom of the second evaporator enters the first reaction kettle from the bottom of the first reaction kettle through the bridging pipeline under the action of pressure difference to have a polymerization condensation reaction, then is discharged from the overflow pipe at the upper part of the first reaction kettle and enters the second reaction kettle from the bottom of the second reaction kettle to have a polymerization condensation reaction, and the modified asphalt obtained after the reaction in the second reaction kettle directly flows into the finished product overhead tank through the upper finished product pipe. With the adoption of the production system and method, the quality of the modified asphalt can be effectively improved and stabilized, and environmental pollution and energy consumption are reduced.
Description
Technical field
The invention belongs to asphalt production technical field, specifically relate to a kind of modified pitch continuous process system and method thereof.
Background technology
Give in the carbon products such as molten anode in production, the material asphalt required need meet following technical indicator: softening temperature SP is 100 ~ 106 DEG C, toluene insolubles BI is 35 ~ 37%, quinoline insolubles QI is 9 ~ 12%, fixed carbon C is 57 ~ 59%, β resin (BI-QI) >=23%, ash A≤0.3%, moisture content W≤5%.
In order to obtain the electrode pitch of above-mentioned high-quality, hot-work upgrading must be carried out to coal-tar pitch.So-called upgrading is exactly that aromatic hydrocarbon molecule in pitch produces hydrogen, methane and water in thermopolymerization and condensation course.Meanwhile, in pitch, a part for original β resin is converted into secondary α resin, and a part for benzene insoluble is converted into secondary β resin, thus makes QI, and BI and β value increase thereupon, and its cohesiveness component content is improved, and pitch obtains upgrading.In the polymer theory of macroscopic view, along with the rising of temperature, unsaturated link(age) on hydrocarbon sticky cyclic cpds ruptures, unstable low molecule official can split away off, remaining molecular structure is in a liquid state at a certain temperature and has thermoplasticity, can be pumped into silk, have good viscosifying power during coking, this adhesive property makes the carbonaceous raw material of dispersion form plasticity paste in electrode moulding process, can suppress the structural timber of different shape.Meanwhile, can coking voluntarily at roasting process medium pitch, the carbonaceous raw material originally disperseed is cemented to the entirety of charcoal, there is required structural strength.
But the production method at present for modified pitch normally adopts step modified pitch Production Flow Chart: three reactors at grade are respectively furnished with a flue gas condensing water cooler, Venturi meter smoke consuming apparatus and medial launder.Hot mid-temperature pitch enters three reactors from still jacking successively, and carry out heating up within the time that mid-temperature pitch does not enter reactor, constant temperature, cooling, then successively from blowing bottom reactor, then deliver to the submerged pump of medial launder that pitch is high puts groove.
Above-mentioned Production Process for Modified Pitch is adopted to exist following not enough: (1) polymerization time is at the polymerization temperature inadequate; (2) quality of modified pitch is unstable; (3) frequent constant speed heating and cooling wanted by reactor, reduce the work-ing life of reaction kettle body life-span and oven inner liner brick; (4) environmental pollution is large; (5) labor strength is large; (6) a large amount of thermosteresis, causes energy consumption to increase.
Summary of the invention
For solving the problem, the invention provides a kind of modified pitch continuous process system and method thereof.Effective raising and stable modified pitch quality, reduce environmental pollution, energy efficient, reduction labor strength.
The present invention is achieved by following technical solution.
A kind of modified pitch continuous process system, comprise second evaporator, the first reactor, the second reactor and pitch is high puts groove, described second evaporator is connected with bottom the first reactor by crane span structure pipeline, first reactor is connected with bottom the second reactor by upflow tube, and described second reactor is connected by the high groove of putting of production tube and pitch.
Described production system also comprises medial launder, and the import of medial launder is connected with crane span structure pipeline, exports and is connected by the high groove of putting of submerged pump and pitch.
Described first reactor is connected the first condenser and the second condenser respectively with the second reactor top, and the first condenser is connected with gas-liquid separator respectively with the second condenser, and gas-liquid separator is connected to Venturi meter and oil groove.
The import of described Venturi meter is high with pitch respectively puts groove and is connected with medial launder.
The outlet of described Venturi meter is also connected with washing column, and is provided with circulation groove in washing column.
Agitator is provided with in described first reactor and the second reactor.
Described first condenser and the second condenser all adopt shell and tube condensate cooler
A kind of modified pitch continuous production method, comprises following method steps:
(1) mid-temperature pitch out bottom second evaporator is entered in the first reactor through crane span structure pipeline under the effect of pressure reduction bottom the first reactor carry out polymeric condensation reaction, then from the upflow tube on the first reactor top out, enter in the second reactor bottom the second reactor and carry out polymeric condensation reaction, the reaction times in the first reactor and the second reactor is 10 ~ 12 hours;
(2) after the second reactor reaction, the modified pitch that obtains flows directly into by the production tube on top that finished product is high puts groove;
The flue gas that (3) first reactors and the second reactor produce enters the first condenser and the cooling of the second condenser respectively, and the gas-liquid phase mixture completely that is not condensed carries out gas-liquid separator, and gas phase flue gas enters Venturi meter, and liquid phase flows into oil groove;
The high all flue gases put in groove of (4) first reactors, the second reactor, medial launder and pitch enter Venturi meter, become white enter air through the washing column washing oil tail gas sprayed after absorption by yellow-green colour.
Described bottom second evaporator mid-temperature pitch temperature be out 280 ~ 300 DEG C.
The end temperature of described first reactor controls within the scope of 335 ~ 380 DEG C, and the flue temperature of the first reactor controls within the scope of 420 ~ 480 DEG C; The end temperature of the second reactor controls within the scope of 395 ~ 410 DEG C, and the second reactor flue temperature is within 380 ~ 430 DEG C.
The invention has the beneficial effects as follows:
Compared with prior art, the present invention has following remarkable advantage:
(1) throughput of modified pitch is substantially increased;
(2) reduce energy consumption, its power consumption, water consumption and coal gas consumption decline 40%;
(3) owing to using continuous processing to produce, steam consumption quantity is corresponding decline 40% due to the increase of throughput; And use steaming out pipeline continually owing to avoiding in process of production, actual steam consumption reduces 80%;
(4) after using continuous processing to produce, not only there is equilibrium in bitumen flue gas, and composition is more stable, no longer there is pressure still and use steaming out, cause the phenomenon that flue gas increases suddenly, and greatly reduce moisture content in flue gas, be so not only conducive to the operational stability of absorption flue gas process but also can prevent because moisture condensation causes washing oil emulsification, thus can ensure that washing oil absorbs normally carrying out of flue gas operation, and the comprehensive utilization that can be flue gas creates conditions;
(5) simplify the operation, alleviate the labour intensity of workman;
(6) work-ing life of reaction kettle body and oven inner liner brick is extended:
(7) Collection and utilization of waste heat is effectively realized;
(8) only need shunt 1/3 during Nai Cai factory dress mid-temperature pitch and enter car, not affect normal production;
(9) Polycondensation Reactor and Esterification Reactor not easily coking.
Accompanying drawing explanation
Fig. 1 is system architecture schematic diagram of the present invention;
Fig. 2 is the graph of a relation of pitch softening point and toluene insolubles, quinoline insolubles and fixed carbon.
In figure: 1-second evaporator, 2-first reactor, 3-second reactor, 4-medial launder, 5-pitch is high puts groove, 6-submerged pump, 7-bridge formation pipeline, 8-upflow tube, 9-production tube, 10-first condenser, 11-second condenser, 12-gas-liquid separator, 13-oil groove, 14-Venturi meter, 15-washing column.
Embodiment
Technical scheme of the present invention is further described below in conjunction with accompanying drawing, but described in claimed scope is not limited to.
As shown in Figure 1, a kind of modified pitch continuous process system of the present invention, comprise second evaporator 1, first reactor 2, second reactor 3 and pitch is high puts groove 5, described second evaporator 1 is connected with bottom the first reactor 2 by crane span structure pipeline 7, first reactor 2 is connected with bottom the second reactor 3 by upflow tube 8, and described second reactor 3 is connected by the high groove 5 of putting of production tube 9 and pitch.Adopt the technical program, the transformation of material continuously from mid-temperature pitch to modified pitch can be realized to modified pitch; This system is equivalent to a large communicating vessels.In process of production, become product through suitable polymeric condensation temperature and suitable polymeric condensation time and overflow, not only ensure that not easily coking at the bottom of still, and ensure that the stable of quality product.Simultaneously need not frequently, heating and cooling rapidly, extend the work-ing life of reactor and oven inner liner brick.
Described production system also comprises medial launder 4, and the import of medial launder 4 is connected with crane span structure pipeline 7, exports and is connected by the high groove 5 of putting of submerged pump 6 and pitch.The effect of medial launder 4 is used as emergent management under shut-down or accidental state, and the pitch putting medial launder 4 is sent to by submerged pump 6 that pitch is high puts groove 5.
Described first reactor 2 and the second reactor 3 top are connected the first condenser 10 and the second condenser 11 respectively, and the first condenser 10 is connected with gas-liquid separator 12 respectively with the second condenser 11, gas-liquid separator 12 is connected to Venturi meter 14 and oil groove 13.Adopt the technical program, in process of production, after the flue gas that first reactor 2 and the second reactor 3 produce enters the first condenser 10 and the cooling of the second condenser 11 respectively, the gas-liquid phase mixture completely that is not condensed enters gas-liquid separator 12 and is separated, gas phase flue gas enters Venturi meter 14, and liquid phase flows into oil groove 13.
The import of described Venturi meter 14 respectively put groove 5 high with pitch is connected with medial launder 4.Like this, the first reactor 2, second reactor 3, medial launder 4 and the high all flue gases put in groove 5 of pitch can be made to enter Venturi meter 14.
The outlet of described Venturi meter 14 is also connected with washing column 15, and is provided with circulation groove in washing column 15.Adopt the technical program, when producing modified pitch, washing column 15 becomes white with the tail gas after washing oil sprinkling absorption by yellow-green colour and enters air, and its four benzopyrenes content is 0.135mg/N.m
3, the environmental evaluation general standard of generally acknowledging according to battery limit (BL), its pollution level belongs to slight pollution.The oils product reclaimed after cooling, after reaching certain reserves, with pumping toward in tar oil depot Special end product groove, export trade after leaving standstill dehydration.Washing oil periodic replacement in circulation groove, ensures good assimilation effect.
Agitator is provided with in described first reactor 2 and the second reactor 3.
Described first condenser 10 and the second condenser 11 all adopt shell and tube condensate cooler
As shown in Figure 1, a kind of modified pitch continuous production method, its method steps is as follows:
(1) mid-temperature pitch out bottom second evaporator 1 is entered in the first reactor 2 through crane span structure pipeline 7 under the effect of pressure reduction bottom the first reactor 2 carry out polymeric condensation reaction, then from the upflow tube 8 on the first reactor 2 top out, enter in the second reactor 3 bottom the second reactor 3 and carry out polymeric condensation reaction, the reaction times in the first reactor 2 and the second reactor 3 is 10 ~ 12 hours;
(2) after the second reactor 3 reacts, the modified pitch that obtains flows directly into by the production tube 9 on top that finished product is high puts groove 5;
The flue gas that (3) first reactors 2 and the second reactor 3 produce enters the first condenser 10 respectively and the second condenser 11 cools, the gas-liquid phase mixture completely that is not condensed carries out gas-liquid separator 12, gas phase flue gas enters Venturi meter 14, and liquid phase flows into oil groove 13;
(4) first reactor 2, second reactors 3, medial launder 4 and the high all flue gases put in groove 5 of pitch enter Venturi meter 14, and the tail gas after washing column 15 sprays absorption with washing oil becomes white by yellow-green colour and enters air.
Described bottom second evaporator 1 mid-temperature pitch temperature be out 280 ~ 300 DEG C.
The end temperature of described first reactor 2 controls within the scope of 335 ~ 380 DEG C, and the flue temperature of the first reactor 2 controls within the scope of 420 ~ 480 DEG C; The end temperature of the second reactor 3 controls within the scope of 395 ~ 410 DEG C, and the second reactor 3 flue temperature is within 380 ~ 430 DEG C.
Adopt aforesaid method, the transformation of material continuously from mid-temperature pitch to modified pitch can be realized to modified pitch; In technological process, have employed fluid mechanics principle, is a large communicating vessels by flow scheme design.Owing to have employed from reactor bottom feed, for liquid substance in still, the liquid that always temperature is lower is in bottom, and moved upward to top by the liquid after flue heats, become product through suitable polymeric condensation temperature and suitable polymeric condensation time to overflow, one is ensure that not easily coking at the bottom of still, and two is ensure that stablizing of quality product.For the flue of reacting by heating still, need not frequently, heating and cooling rapidly, extend the work-ing life of reactor and oven inner liner brick; Eliminate in former technical process simultaneously and pollute maximum, that operation easier is maximum, labour intensity is maximum medial launder link, shorten flow process, the medial launder 4 in this technical scheme is just as stopping work or Emergency use under malfunction.
In the above-mentioned methods, as shown in Figure 1, the pressure reduction that the weight that the pressure reduction that the weight that the pressure reduction of A, B 2 deducts pitch in the first reactor 2 also remains deducts pitch in the second reactor 3 much larger than the pressure reduction of B, C 2 also remains; That is: Δ P
1> > Δ P
2.
Adopt technique scheme, can save power consumption 10-20%, gas saving consumes 35-40%, saves purging steam 80%.
The continuous processing production technique of this modified pitch with hydromechanical fundamental equation (bernoulli equation) for theoretical foundation: Z
1+ U
1 2/ 2g+P
1/ ρ g=Z
2+ U
2 2/ 2g+P
2/ ρ P, whole technical process is equivalent to a large communicating vessels, and as shown in Figure 1, in Fig. 1, the flow velocity of A, B, C 3 can be similar to and be considered as equal, and is a running balance value, so above formula can be changed into: △ P=P
2-P
1=(Z2-Z1) ρ g.
In above formula, △ P is P
1, P
2pressure reduction, P
1for the pressure of A point, P
2for the pressure of B point;
G is universal gravity constant, and unit is m/S
2, value is 9.81;
ρ is asphalt density, and unit is t/m
3, value is about 1.6;
Z
1for A point is apart from the height on ground, Z
2for B point is apart from the height on ground, unit is m.
As shown in Figure 1, the pressure reduction that the pressure reduction that A, B are 2 obtains after deducting the weight of liquid in the first reactor 2, the pressure reduction obtained after the pressure reduction that can be greater than B, C 2 deducts the weight of liquid in the second reactor 3, therefore, the liquid in this communicating vessels can continuously flow.
In the technical program, the order of modified pitch quality index impact is: Temperature-time-pressure.
Best manufacturing condition is obtained for finding operating time, temperature, pressure and interaction thereof to the impact of modified pitch indices.The mid-temperature pitch that have employed same softening temperature makes raw material, carries out positive quadraturing design test, carry out intiutive analysis method by mass data by Three factors two level, obtains the interact relation table of temperature, pressure, time and modified pitch indices, in table 1.
As seen from Table 1, service temperature, pressure, time are different on the impact of modified pitch quality index.Wherein, being maximum with the impact of service temperature, is secondly the time, is pressure again.
Table 1
| Modified pitch index | Affect primary and secondary order: main → secondary |
| Softening temperature (SP) DEG C | Temperature → pressure × time → temperature × time → pressure → temperature × pressure → time |
| Benzene insoluble (BI) % | Temperature → pressure × time → time → temperature × time → temperature × pressure → pressure |
| Quinoline insolubles (QI) % | Temperature → pressure → pressure × time → time → temperature × time → temperature × pressure |
| Fixed carbon (C) % | Temperature → pressure × time → time → temperature × time → temperature × pressure → pressure |
| Net effect | Temperature → pressure × time → time → temperature × time → temperature × pressure → pressure |
By the test operation data of table 1, the relation of pitch softening point and toluene insolubles BI, quinoline insolubles QI and fixed carbon C can be obtained as shown in Figure 2.
As can be seen from Figure 2, when softening temperature within the scope of 100-106 DEG C in corresponding benzene insolubles be 35.8-36.2%, fixed carbon is 57.3-59.2%, and in quinoline, insolubles is 8.8-12.5%, reaches all technical required by modified pitch.
By the relation that table 1 and Fig. 2 obtain, be specifically applied in the method for the invention and can obtain as drawn a conclusion:
(1) because the technical program adopts normal pressure operate continuously, therefore the pressure of the first reactor 2 and the second reactor 3 is constant, and is normal pressure.Because reactor volume is fixed, the dnockout amount of tar one, two sections of pumps is also certain, in the metastable situation of quality of coke tar, the generating capacity of pitch is certain, therefore polymerization time is at the polymerization temperature certain, namely 10 ~ 12 hours (because mid-temperature pitch enters the first reactor 2 and is just in polymerization state).
(2) BI%, QI%, C% content in pitch index is along with the rising of polymerization temperature (softening temperature), the prolongation of time and increasing substantially.
According to above 2 conclusions, the relation obtaining modified pitch operation index and pitch softening point is as shown in table 2 below.Can be found out by table 2, along with the rising reactor liquidus temperature of flue temperature increases, softening temperature is also along with raising; Adopt method of the present invention to carry out modified pitch production run test, product reaches index as shown in table 3 below.
Table 2
Table 3
| Test number (TN) | SP℃ | BI％ | QI％ | P％ | C％ | A％ | W％ |
| Test one | 109.63 | 27.67 | 7.10 | 20.57 | 53.53 | 0.10 | 2.38 |
| Test two | 107.93 | 27.30 | 7.48 | 19.82 | 51.98 | 0.09 | 2.40 |
| Test three | 105.73 | 28.22 | 8.36 | 19.86 | 53.02 | 0.074 | 2.32 |
| Test four | 108.77 | 27.68 | 7.79 | 19.89 | 53.53 | 0.11 | 2.10 |
| Test five | 108.59 | 28.07 | 8.65 | 19.42 | 54.02 | 0.09 | 2.08 |
| Test six | 112.63 | 29.98 | 9.45 | 20.53 | 54.97 | 0.10 | 2.25 |
As can be seen from Table 3, shown by testing data, adopt the present invention to produce the state quality standard GB8730-83 that modified pitch daily mean fullys meet modified pitch.
But in order to meet quality product requirement, add in finished product a small amount of anthracene oil or
oil adjustable pitch softening point and do not affect other physical and chemical index, meets arithmetic additivity principle.Equally, the quality index that liquid-phase mixing is deposited of different pitches also meets arithmetic additivity principle, so, for ensureing quality product and stability, need if desired to allocate finished product.
For meeting the visual appearance of product: require finished product strip solid for Ф 8-12 after cooling curing is shaping, so require that the blowing temperature of pitch is advisable at about 190 DEG C, finished asphalt powdering can be avoided like this or in open column shape, thus ensure pitch outer, intensity and moisture.
Adopt method of the present invention, substantially increase the throughput of modified pitch, table 4 is the production data to the pitch in May 4 in 1997 in 1992.As can be seen from Table 4, from 1992 to the end of the year 1996, the overall yield of modified pitch is 50.19%.And after using continuous processing to produce, the productive rate of modified pitch is 56%, then productive rate improves 5.8%.By the calculating of annual process 31000 tons, tar, modified pitch 31000 × 5.8%=18000 can be produced every year more.If modified pitch selling price is by 1000 yuan of values, then can increase benefit 1800 × 1000.00=180 ten thousand yuan every year.
Table 4
| Time | Tar processing amount (t) | Modified pitch output (t) | Modified pitch productive rate (%) |
| 1992 | 30119 | 15274 | 50.71 |
| 1993 | 39682 | 15102 | 50.88 |
| 1994 | 33470 | 18213 | 54.42 |
| Nineteen ninety-five | 30318 | 14797 | 48.80 |
| The 4-11 month in 1996 | 18933 | 8186 | 43.03 |
| In March ,-1997 in December, 1996 | 14177 | 7940 | 56.00 |
Claims (10)
1. a modified pitch continuous process system, it is characterized in that: comprise that second evaporator (1), the first reactor (2), the second reactor (3) and pitch are high puts groove (5), described second evaporator (1) is connected with the first reactor (2) bottom by crane span structure pipeline (7), first reactor (2) is connected with the second reactor (3) bottom by upflow tube (8), and described second reactor (3) is connected by the high groove (5) of putting of production tube (9) and pitch.
2. a kind of modified pitch continuous process system according to claim 1, it is characterized in that: described production system also comprises medial launder (4), the import of medial launder (4) is connected with crane span structure pipeline (7), exports and is connected by the high groove (5) of putting of submerged pump (6) and pitch.
3. a kind of modified pitch continuous process system according to claim 1, it is characterized in that: described first reactor (2) and the second reactor (3) top are connected the first condenser (10) and the second condenser (11) respectively, and the first condenser (10) is connected with gas-liquid separator (12) respectively with the second condenser (11), gas-liquid separator (12) is connected to Venturi meter (14) and oil groove (13).
4. a kind of modified pitch continuous process system according to claim 3, is characterized in that: the import of described Venturi meter (14) respectively put groove (5) high with pitch is connected with medial launder (4).
5. a kind of modified pitch continuous process system according to claim 3, is characterized in that: the outlet of described Venturi meter (14) is also connected with washing column (15), and is provided with circulation groove in washing column (15).
6. a kind of modified pitch continuous process system according to claim 1, is characterized in that: be provided with agitator in described first reactor (2) and the second reactor (3).
7. a kind of modified pitch continuous process system according to claim 3, is characterized in that: described first condenser (10) and the second condenser (11) all adopt shell and tube condensate cooler.
8. a modified pitch continuous production method, is characterized in that: comprise following method steps:
(1) polymeric condensation reaction is carried out by entering in the first reactor (2) from the first reactor (2) bottom through crane span structure pipeline (7) under the effect of pressure reduction from second evaporator (1) bottom mid-temperature pitch out, then from the upflow tube (8) on the first reactor (2) top out, enter in the second reactor (3) carry out polymeric condensation reaction from the second reactor (3) bottom again, the reaction times in the first reactor (2) and the second reactor (3) is 10 ~ 12 hours;
(2) after the second reactor (3) reaction, the modified pitch that obtains flows directly into by the production tube (9) on top that finished product is high puts groove (5);
The flue gas that (3) first reactors (2) and the second reactor (3) produce enters the first condenser (10) and the second condenser (11) cooling respectively, the gas-liquid phase mixture completely that is not condensed carries out gas-liquid separator (12), gas phase flue gas enters Venturi meter (14), and liquid phase flows into oil groove (13);
The high all flue gases put in groove (5) of (4) first reactors (2), the second reactor (3), medial launder (4) and pitch enter Venturi meter (14), and the tail gas after washing column (15) sprays absorption with washing oil becomes white by yellow-green colour and enters air.
9. a kind of modified pitch continuous production method according to claim 8, is characterized in that: described from second evaporator (1) bottom mid-temperature pitch temperature be out 280 ~ 300 DEG C.
10. a kind of modified pitch continuous production method according to claim 8, it is characterized in that: the end temperature of described first reactor (2) controls within the scope of 335 ~ 380 DEG C, the flue temperature of the first reactor (2) controls within the scope of 420 ~ 480 DEG C; The end temperature of the second reactor (3) controls within the scope of 395 ~ 410 DEG C, and the second reactor (3) flue temperature is within 380 ~ 430 DEG C.
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| CN108424780A (en) * | 2018-03-06 | 2018-08-21 | 国家能源投资集团有限责任公司 | Modified pitch and its continuous producing method and system |
| CN108641740A (en) * | 2018-05-31 | 2018-10-12 | 山西豪仑科化工有限公司 | A kind of modified coal tar pitch and preparation method and application by alternating temperature production of pressurizeing |
| CN110396421A (en) * | 2019-08-19 | 2019-11-01 | 七台河宝泰隆新能源有限公司 | A kind of preventing mean and method of restructuring asphalt tower pipeline coking and blocking pipeline |
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| CN108641740A (en) * | 2018-05-31 | 2018-10-12 | 山西豪仑科化工有限公司 | A kind of modified coal tar pitch and preparation method and application by alternating temperature production of pressurizeing |
| CN110396421A (en) * | 2019-08-19 | 2019-11-01 | 七台河宝泰隆新能源有限公司 | A kind of preventing mean and method of restructuring asphalt tower pipeline coking and blocking pipeline |
| CN110396421B (en) * | 2019-08-19 | 2024-02-02 | 七台河宝泰隆新能源有限公司 | Device and method for preventing coking and blockage of modified asphalt tower pipeline |
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| CN105331384B (en) | 2018-03-09 |
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