CN208898797U - A kind of equipment that the separation of coal pyrolysis gas is integrated with energy regenerating - Google Patents
A kind of equipment that the separation of coal pyrolysis gas is integrated with energy regenerating Download PDFInfo
- Publication number
- CN208898797U CN208898797U CN201820941950.8U CN201820941950U CN208898797U CN 208898797 U CN208898797 U CN 208898797U CN 201820941950 U CN201820941950 U CN 201820941950U CN 208898797 U CN208898797 U CN 208898797U
- Authority
- CN
- China
- Prior art keywords
- oil
- carbolineum
- tower
- fractionating column
- stripper
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to the equipment that a kind of separation of coal pyrolysis gas and energy regenerating integrate, and follow system by column bottoms pump, II carbolineum pump follows system, I carbolineum pump follows system, washing oil pump follows system and effectively recycled with the energy of pyrolysis gas.Coal gas after separation is produced from oil wash fractionating column condenser, and light oil, carbolic oil, naphtalene oil tri-mixed fractions enter the separation extraction of normal pressure knockout tower, and washing oil, I carbolineum, II carbolineum produce after being stripped by oil wash fractionating column side line, and heavy oil is produced by tower bottom.After separating by process energy recycling with product, product purity is high, and energy recovery rate is high.The utility model is by oil wash fractionation process a little, it is possible to reduce the treating capacity of phenol wastewater reduces the difficulty of water-oil separating, reduces cost of equipment, realizes effective recycling of energy, and product purity is high.Use scope is wide, also can be used for the pyrogenation and carbonization product separation of oil-sand, oil shale, waste tire, petroleum coke, organic waste materials and biomass.
Description
Technical field
The utility model relates to pyrolysis of coal retorting technique fields, are a kind of points of coal pyrolysis gas (raw coke oven gas) specifically
Equipment from being integrated with energy regenerating.
Background technique
China belongs to the country that oil starvation lacks gas, and petroleum, natural gas resource are deficient, coal resources relative abundance.Coal conduct
The main body energy and the important raw material of industry in China occupy critical role in China's non-renewable energy production and consumption structure.Heat
Solution refers to be heated in the absence of air conditions, and by a series of physical change and chemical reaction, coal generates coal gas, coal
The products such as tar, coke and semicoke, be it is a kind of cleaning, efficient coal utilization effective way.
Currently, being broadly divided into indirectly cooling and directly two kinds of cooling to the technique of pyrolysis of coal oil gas progress refrigerated separation recycling
Method, wherein direct cooling technique is divided into washing and two kinds of oil wash again.Wherein, the indirect cooling recycling tar is referred mainly to water
Or air and pyrolysis oil gas indirect contact heat exchanger realize the separation and recovery of tar.And directly cooling recycling tar be primarily referred to as with
Water or oil realize the separation and recovery of tar as cooling medium and pyrolysis oil gas direct contact heat transfer.
103013583 A of CN proposes that a kind of pyrolysis coal gas dust removal is cooling and tar recovery process, passes through indirectly cooling
Technique realizes the recovery method of tar.The major way separated by heat exchanger and waste heat recovery furnace as tar condensing, together
When alternative scheme provided with accident chilling tower as waste heat recovery furnace.Indirect cooling method can the process that waste heat recycles simultaneously
The condensation for realizing tar and water, can effectively recycle tar.But that there are cooling equipment is big, be easy blocking, heat is difficult to recycle
The problems such as utilization.
105779023 A of CN proposes a kind of pyrolysis coal gas residual neat recovering system and method, in traditional ammonia spray work
It is improved on the basis of skill, can recycle 400 DEG C or more of coal gas heat, and the heat of 20-80 DEG C of part has been carried out time
It receives and utilizes.Although being improved ammonia spray technique, the recycling of portion of energy is also achieved, there are still efficiency of dust collections
Low, ammonia spray amount is big, and how difficult generation wastewater flow rate is, and water-oil separating is difficult, and most of heat is difficult to the problem of recycling.
104498106 A of CN proposes a kind of coal pyrolysis gas tar reclaimer and method, passes through circulation tar recovery tower
It realizes the initial gross separation of tar and realizes that the energy regenerating of high temperature section utilizes by the first second circulation pipeline.This method solves
The problem of heavy tar large viscosity, but the initial gross separation of tar is only realized, the tar after separation also needs by subsequent
The separation for the treatment of process realization light oil, carbolic oil, naphtalene oil, washing oil, carbolineum and heavy oil.
105779028 A of CN proposes the raw coke oven gas heat based on washing rectifying and changes the method for producing and recycling simultaneously, passes through
Rectifying removing heavy tar and coke powder are washed, higher boiling oil product and high temperature raw coke oven gas are obtained, while recycling heat and generating high pressure steaming
Vapour.But the process flow is complicated, is just able to achieve the separation of oil product and the recycling of energy by multitower separation, reforming equipment expense compared with
It is high.The method and apparatus that the separation of coal pyrolysis gas (raw coke oven gas) and energy regenerating integrate.
Utility model content
The purpose of this utility model is to provide the high coals of a kind of processing convenience, good separating effect, energy regenerating utilization rate
The method and apparatus that the separation of pyrolysis gas (raw coke oven gas) and energy regenerating integrate.The method of the utility model can be realized pyrolysis of coal
The separation of gas (raw coke oven gas), while realizing the recycling of the different temperature zones of coal pyrolysis gas energy.
The technology of the utility model is as follows:
A kind of equipment that the separation of coal pyrolysis gas is integrated with energy regenerating, including oil wash fractionating column (3), tower bottom circulating pump
(5), tower bottom circulation heat exchanger (7), II carbolineum circulating pump (10), II carbolineum circulation heat exchanger (12), I carbolineum circulating pump (15),
I carbolineum circulation heat exchanger (17), washing oil circulating pump (20), washing oil circulation heat exchanger (22), tower top circulating pump (25), tower top circulation
Heat exchanger (27), II carbolineum stripper (29), I carbolineum stripper (33), washing oil stripper (37), condenser (42), storage tank
(44), normal pressure knockout tower (48), reboiler (51), complete condenser (54)；It is pyrolyzed oil gas and enters oil wash fractionating column (3) from bottom；
By pipeline connection oil wash fractionating column (3) and II carbolineum circulating pump (10) by II carbolineum circulation heat exchanger (12) it
Return to oil wash fractionating column (3) afterwards；
By pipeline connection oil wash fractionating column (3) and I carbolineum circulating pump (15) by after I carbolineum circulation heat exchanger (17)
It returns oil wash fractionating column (3)；
By pipeline connection oil wash fractionating column (3) with washing oil circulating pump (20) by being returned after washing oil circulation heat exchanger (22)
Fractionating column (3) are washed in oil return；
By pipeline connection oil wash fractionating column (3) and II carbolineum stripper (29), II carbolineum stripper tower bottom is equipped with logistics
Extraction, top gaseous phase return to oil wash fractionating column (3)；
By pipeline connection oil wash fractionating column (3) and I carbolineum stripper (33), I carbolineum stripper tower bottom is adopted equipped with logistics
Out, top gaseous phase returns to oil wash fractionating column (3)；
By pipeline connection oil wash fractionating column (3) and washing oil stripper (37), washing oil stripper tower bottom is produced equipped with logistics,
Top gaseous phase returns to oil wash fractionating column (3)；
By pipeline connection oil wash fractionating column (3) and condenser (42), enter storage tank (44) after condenser (42), storage
Tank is equipped with logistics extraction and part returns to oil wash fractionating column (3) and partially enters normal pressure knockout tower (48)；
Normal pressure knockout tower (48) and reboiler (51) and complete condenser (54) are connected by pipeline, and equal in tower top tower bottom survey line
It is produced equipped with logistics.
Moreover, the oil wash fractionation column pressure on top surface is 0.9-1.4bar, tower reactor pressure is 1-1.8bar, and tower top temperature is
80-140 DEG C, column bottom temperature is 342-392 DEG C.
Moreover, the atmospheric fractional tower tower top pressure is 0.9-1.4bar, tower reactor pressure is 1-1.5bar, and tower top temperature is
70-100 DEG C, column bottom temperature is 200-250 DEG C, and complete condenser temperature is 20-70 DEG C.
Moreover, the oil wash fractionating column has 12-100 block theoretical plate, II carbolineum side take-off position is 6-77 block reason
By plate, I carbolineum side take-off position is 4-56 block theoretical plate, and washing oil side take-off position is 3-36 block reason theoretical plate.
Moreover, it is 8-91 block theoretical plate that the oil wash fractionating column column bottoms pump, which follows extraction position, II carbolineum pump follows extraction position
Setting is 6-77 block theoretical plate, and it is 4-56 block theoretical plate that I carbolineum pump, which follows extraction position, and it is 3-36 that washing oil pump, which follows extraction position,
Block theoretical plate, it is 3-15 block theoretical plate that tower top pump, which follows extraction position,.
Moreover, the oil wash fractionating column condenser temperature is 20-70 DEG C, reflux ratio 0.0005-0.5.
Moreover, the oil wash fractionating column II carbolineum stripper number of theoretical plate is 2-15 block, I carbolineum stripper number of theoretical plate is
2-15 block, washing oil stripper number of theoretical plate 2-15 block.
Moreover, the oil wash fractionation column bottoming cycle temperature is 266-346 DEG C, II carbolineum circulating temperature is 212-298 DEG C,
I carbolineum circulating temperature is 166-246 DEG C, and washing oil circulating temperature is 120-200 DEG C, and tower top circulating temperature is 90-155 DEG C.
Moreover, the atmospheric fractional tower has 5-40 block theoretical plate, it is 2-20 block that carbolic oil, which produces position,.
Moreover, the atmospheric fractional tower complete condenser temperature is 20-70 DEG C, reflux ratio 0.5-10.
The advantages of the utility model and good effect are as follows:
The utility model handles that coal class is more, and the pyrolysis of coal product (raw coke oven gas) of different pyrogenation and carbonization techniques can be with
The generation of waste water is effectively reduced, the cooling equipment of solution is big, the problem of water-oil separating difficulty, passes through simply and easily technique and realizes production
The recycling of the clear separation and energy of product.
Detailed description of the invention
Fig. 1 is the separation of the utility model coal pyrolysis gas (raw coke oven gas) and the method and process flow chart that energy regenerating integrates.
The meaning of figure label is described as follows:
1- coal pyrolysis gas (raw coke oven gas), 2- tower bottom stripped vapor, 3- oil wash fractionating column, 4- column bottoms pump follow extraction logistics, 5-
Tower bottom circulating pump, logistics after 6- tower bottom circulating pump, 7- tower bottom circulation heat exchanger, 8- tower bottom are recycled back into logistics, 9-II carbolineum pump
Follow extraction logistics, 10-II carbolineum circulating pump, logistics after 11-II carbolineum circulating pump, 12-II carbolineum circulation heat exchanger, 13-II anthracene
Oil is recycled back into logistics, and 14-I carbolineum, which pumps, follows extraction logistics, 15-I carbolineum circulating pump, logistics after 16-I carbolineum circulating pump, 17-I
Carbolineum circulation heat exchanger, 18-I carbolineum are recycled back into logistics, and 19- washing oil pump follows extraction logistics, 20- washing oil circulating pump, 21- washing oil
Logistics after circulating pump, 22- washing oil circulation heat exchanger, 23- washing oil are recycled back into logistics, the circulation extraction logistics of 24- tower top, 25- tower
Circulating pump is pushed up, logistics after 26- tower top circulating pump, 27- tower top circulation heat exchanger, 28- tower top is recycled back into logistics, 29-II carbolineum
Stripper, the stripping extraction logistics of 30-II carbolineum, 31-II carbolineum stripped vapor, 32-II carbolineum strip return logistics, 33-I anthracene
Oil and gas stripper, the stripping extraction logistics of 34-I carbolineum, 35-I carbolineum stripped vapor, 36-I carbolineum strip return logistics, 37- washing oil vapour
Stripper, the stripping extraction logistics of 38- washing oil, 39- washing oil stripped vapor, 40- washing oil stripping return logistics, 41- overhead extraction logistics,
42- condenser, logistics after 43- condensation, 44- storage tank, 45- overhead condensation liquid phase, 46- overhead condensate reflux logistics, 47- tower top are cold
Solidifying extraction logistics, 48- normal pressure knockout tower, 49- tower bottom produce logistics, and 50- tower bottom recycles logistics, 51- reboiler, and 52- tower bottom is returned
Logistics is returned, 53- normal pressure knockout tower produces logistics, 54- complete condenser, 55- overhead condensation logistics, 56- overhead reflux logistics, 57- coal
Gas, 58- light oil, 59- carbolic oil, 60- naphtalene oil, 61- washing oil, 62-I carbolineum, 63-II carbolineum, 64- heavy oil.
Specific embodiment
It is further detailed below in conjunction with method and apparatus of the attached drawing to the offer of the utility model.The utility model
It is achieved by the following technical solution:
A kind of equipment that the separation of coal pyrolysis gas (raw coke oven gas) is integrated with energy regenerating, as shown in Figure 1, including that oil wash is fractionated
Tower 3, tower bottom circulating pump 5, tower bottom circulation heat exchanger 7, II carbolineum circulating pump 10, II carbolineum circulation heat exchanger 12, I carbolineum circulating pump
15, I carbolineum circulation heat exchanger 17, washing oil circulating pump 20, washing oil circulation heat exchanger 22, tower top circulating pump 25, tower top cycle heat exchange
Device 27, II carbolineum stripper 29, I carbolineum stripper 33, washing oil stripper 37, condenser 42, storage tank 44, normal pressure knockout tower 48,
Reboiler 51, complete condenser 54；
Coal pyrolysis gas (raw coke oven gas) is included in oil wash fractionating column 3 from tower bottom, connects oil wash fractionating column 3 by pipeline and follows with tower bottom
Ring pump 5 is by returning to oil wash fractionating column 3 after tower bottom circulation heat exchanger 7；
Oil wash fractionating column 3 and II carbolineum circulating pump 10 are connected by returning after II carbolineum circulation heat exchanger 12 by pipeline
Oil wash fractionating column 3；
Oil wash fractionating column 3 and I carbolineum circulating pump 15 are connected by returning to oil after I carbolineum circulation heat exchanger 17 by pipeline
Wash fractionating column 3；
Oil wash fractionating column 3 and washing oil circulating pump 20 are connected by returning to oil wash after washing oil circulation heat exchanger 22 by pipeline
Fractionating column 3；
Oil wash fractionating column 3 and II carbolineum stripper 29 are connected by pipeline, II carbolineum stripper tower bottom is produced equipped with logistics,
Top gaseous phase returns to oil wash fractionating column 3；
Oil wash fractionating column 3 and I carbolineum stripper 33 are connected by pipeline, I carbolineum stripper tower bottom is produced equipped with logistics, tower
Top gas mutually returns to oil wash fractionating column 3；
Oil wash fractionating column 3 and washing oil stripper 37 are connected by pipeline, washing oil stripper tower bottom is produced equipped with logistics, tower top
Gas phase returns to oil wash fractionating column 3；
Oil wash fractionating column 3 and condenser 42 are connected by pipeline, storage tank 44 is entered after condenser 42, storage tank is equipped with object
Stream extraction and part return to 3 part of oil wash fractionating column and enter normal pressure knockout tower 48；
Normal pressure knockout tower 48 and reboiler 51 and complete condenser 54 are connected by pipeline, and is equipped with object in tower top tower bottom survey line
Stream extraction.
Experiments prove that: above-mentioned circulation is directed to the position of tower body are as follows: washing oil circulation is located substantially at 25-30%, I anthracene
Oil circulation is located at 40-50%, and II carbolineum circulation is located at 60-70%, and tower reactor pump is followed positioned at 90% or more.
The process of the utility model, is described as follows:
Coal pyrolysis gas (raw coke oven gas) 1 and tower bottom stripped vapor 2 enter oil wash fractionating column 3 by bottom respectively,
(1) tower bottom circulation logistics 4 is produced by oil wash fractionating column 3 to return after tower bottom circulating pump 5 and tower bottom circulation heat exchanger 7
Fractionating column 3 is washed in oil return；
(2) extraction logistics 9 is followed by II carbolineum circulating pump 10 and II carbolineum circulation by the extraction II carbolineum pump of oil wash fractionating column 3
Oil wash fractionating column 3 is returned after heat exchanger 12；
(3) I carbolineum pump is produced by oil wash fractionating column 3 and follows extraction logistics 14 by I carbolineum circulating pump 15 and I carbolineum circulating picture-changing
Oil wash fractionating column 3 is returned after hot device 17；
(4) washing oil circulation extraction logistics 19 is produced by washing oil circulating pump 20 and washing oil cycle heat exchange by oil wash fractionating column 3
Washing oil fractionating column 3 is returned after device 22；
(5) tower top circulation extraction logistics 24 is produced by tower top circulating pump 25 and tower top cycle heat exchange by oil wash fractionating column 3
Oil wash fractionating column 3 is returned after device 27；
(6) the stripping extraction logistics 30 of II carbolineum is produced by oil wash fractionating column 3 and enters the extraction of 29,29 bottom of II carbolineum stripper
II anthracene oil product 63, II carbolineum stripped vapor 31 enter 29 by bottom, and 32 return to oil wash fractionating column 3 after stripping；
(7) the stripping extraction logistics 34 of I carbolineum is produced by oil wash fractionating column 3 and enters 33,33 bottom of I carbolineum stripper extraction I
Anthracene oil product 62, I carbolineum stripped vapor 35 enter 33 by bottom, and 36 return to oil wash fractionating column 3 after stripping；
(8) washing oil stripping extraction logistics 38 is produced by oil wash fractionating column 3 and enters 37,37 bottom of washing oil stripper extraction washing oil
Product 61, washing oil stripped vapor 39 enter 37 by bottom, and 40 return to oil wash fractionating column 3 after stripping；
(9) 3 tower bottom of oil wash fractionating column produces heavy oil product 64；
(10) 3 overhead extraction gas phase 41 of oil wash fractionating column enters condenser 42, after the storage separation of storage tank 44, produces coal
Gas 57, and overhead condensate reflux logistics 46 returns to 3, overhead extraction logistics 47 enters normal pressure knockout tower 48；
(11) the 48 overhead extraction logistics 53 of normal pressure knockout tower partially returns to 48 after complete condenser 54 while producing light oil production
Product 58；
(12) 48 side take-off carbolic oil product 59 of normal pressure knockout tower；
(13) 48 tower reactor of normal pressure knockout tower extraction 49 part of logistics returns to 48 by reboiler 51 and produces naphtalene oil product simultaneously
60；
The method and apparatus that the separation of the coal pyrolysis gas (raw coke oven gas) of the utility model and energy regenerating integrate, is pyrolysis oven
High temperature pyrolysis of oil and gas out without it is cooling be directly entered oil wash fractionation column base, coal gas and light oil carbolic oil naphtalene oil tri-mixed fractions from
Oil wash fractionating column produces and passes through normal pressure knockout tower further isolated tri-mixed fractions；Washing oil, I carbolineum and II carbolineum pass through oil
It washes fractionating column side line and is used as product out by stripper；Heavy oil product is produced by oil scrubber tower bottom；Multiple pumps are arranged in oil scrubber
The energy for receiving coal pyrolysis gas (raw coke oven gas) different temperature zones is walked around to, can produce the saturated vapor of different pressures；Tower bottom circulation warm
Degree is 266-346 DEG C, and II carbolineum circulating temperature is 212-298 DEG C, and I carbolineum circulating temperature is 166-246 DEG C, washing oil circulating temperature
It is 120-200 DEG C, tower top circulating temperature is 90-155 DEG C, and oil wash fractionating column has 12-100 block theoretical plate, tower top temperature 80-
140 DEG C, column bottom temperature is 342-392 DEG C, and condenser temperature is 20-70 DEG C；Normal pressure knockout tower has 5-40 block theoretical plate, tower top
Temperature is 70-100 DEG C, and column bottom temperature is 200-250 DEG C, and complete condenser temperature is 20-70 DEG C, and it is 2-20 block that carbolic oil, which produces position,.
Wherein II carbolineum side take-off position is 6-77 block theoretical plate, and I carbolineum side take-off position is 4-56 block reason
By plate, washing oil side take-off position is 3-36 block reason theoretical plate, and it is 8-91 block theoretical plate, II anthracene that column bottoms pump, which follows extraction position,
It is 6-77 block theoretical plate that oil pump, which follows extraction position, and it is 4-56 block theoretical plate that I carbolineum pump, which follows extraction position, and washing oil pump follows extraction
Position is 3-36 block theoretical plate, and it is 3-15 block theoretical plate that tower top pump, which follows extraction position,.
II carbolineum stripper number of theoretical plate is 2-15 block, and I carbolineum stripper number of theoretical plate is 2-15 block, washing oil stripper reason
By plate number 2-15 block.
Oil wash fractionating column reflux ratio is 0.0005-0.5, and normal pressure knockout tower reflux ratio is 0.5-10.
Oil wash fractionation column pressure on top surface is 0.9-1.4bar, and tower reactor pressure is 1-1.8bar, atmospheric fractional tower tower top pressure
For 0.9-1.4bar, tower reactor pressure is 1-1.5bar.
Tower bottom circulating temperature is 266-346 DEG C, and II carbolineum circulating temperature is 212-298 DEG C, and I carbolineum circulating temperature is 166-
246 DEG C, washing oil circulating temperature is 120-200 DEG C, and tower top circulating temperature is 90-155 DEG C；Oil wash fractionating column has 12-100 block
Theoretical plate, tower top temperature are 80-140 DEG C, and column bottom temperature is 342-392 DEG C, and condenser temperature is 20-70 DEG C；II carbolineum side line
Producing position is 6-77 block theoretical plate, and I carbolineum side take-off position is 4-56 block theoretical plate, and washing oil side take-off position is
3-36 block manages theoretical plate, and it is 8-91 block theoretical plate that column bottoms pump, which follows extraction position, and it is 6-77 that II carbolineum pump, which follows extraction position,
Block theoretical plate, it is 4-56 block theoretical plate that I carbolineum pump, which follows extraction position, and it is 3-36 block theoretical plate that washing oil pump, which follows extraction position,
It is 3-15 block theoretical plate that tower top pump, which follows extraction position, and II carbolineum stripper number of theoretical plate is 2-15 block, and I carbolineum stripper is theoretical
Plate number is 2-15 block, washing oil stripper number of theoretical plate 2-15 block；Normal pressure knockout tower has 5-40 block theoretical plate, and tower top temperature is
70-100 DEG C, column bottom temperature is 200-250 DEG C, and complete condenser temperature is 20-70 DEG C, and it is 2-20 block that carbolic oil, which produces position,；Oil scrubber
Reflux ratio is 0.0005-0.5, and normal pressure knockout tower reflux ratio is 0.5-10；Oil wash fractionation column pressure on top surface is 0.9-1.4bar, tower
Kettle pressure is 1-1.8bar, and normal pressure knockout tower tower top pressure is 0.9-1.4bar, and tower reactor pressure is 1-1.5bar.
Embodiment 1
The utility model method is used for separation and the energy regenerating of coal pyrolysis gas, coal pyrolysis gas treating capacity is 60 tons/it is small
When, it is identical as the utility model process, including oil wash fractionating column, tower bottom circulating pump, tower bottom circulation heat exchanger, II carbolineum circulation
Pump, II carbolineum circulation heat exchanger, I carbolineum circulating pump, I carbolineum circulation heat exchanger, washing oil circulating pump, washing oil circulation heat exchanger, tower
Push up circulating pump, tower top circulation heat exchanger, II carbolineum stripper, I carbolineum stripper, washing oil stripper, condenser, storage tank, normal pressure
Knockout tower, reboiler, complete condenser.
Oil wash fractionation column pressure on top surface is 0.9bar, and tower reactor pressure is 1bar.Oil wash fractionating column totally 12 pieces of theoretical plates, it is resonable
Enter washing oil stripper by side take-off at plate 3, side take-off enters I carbolineum stripper at theoretical plate 4, at theoretical plate 6
Side take-off enters II carbolineum stripper, and tower top pump is produced at theoretical plate 2 and follows logistics, is taken by tower bottom circulation heat exchanger
Heat produces washing oil pump at theoretical plate 3 and follows logistics, carries out taking heat by washing oil circulation heat exchanger, I anthracene is produced at theoretical plate 4
Oil pump follows logistics, carries out taking heat by I carbolineum circulation heat exchanger, and II carbolineum pump is produced at theoretical plate 6 and follows logistics, passes through II
Carbolineum circulation heat exchanger carries out taking heat, and column bottoms pump is produced at theoretical plate 8 and follows logistics, is taken by tower bottom circulation heat exchanger
Heat.Washing oil stripper, I carbolineum stripper and II carbolineum stripper have 2 pieces of theoretical plates.Reflux ratio is 0.5.
Oil wash fractionator overhead temperature is 80 DEG C, and bottom temperature is 342 DEG C, and segregator temperature is 20 DEG C.
It is 266 DEG C that column bottoms pump, which follows extraction temperature, and it is 212 DEG C that II carbolineum pump, which follows extraction temperature, and I carbolineum pump follows extraction temperature and is
166 DEG C, it is 120 DEG C that washing oil pump, which follows extraction temperature, and tower top circulating temperature is 90 DEG C.
Atmospheric fractional tower has 5 pieces of theoretical plates, and it is tower top pressure 0.9bar at 2 pieces of theoretical plates, tower reactor that carbolic oil, which produces position,
Pressure is 1bar, reflux ratio 10.
Atmospheric fractional tower tower top temperature is 70 DEG C, and bottom temperature is 200 DEG C, and complete condenser temperature is 20 DEG C.
266 DEG C of heat 7.6Gcal can be recycled per hour, recycle 212 DEG C of heat 2.2Gcal, recycle 166 DEG C of heats
1.2Gcal recycles 120 DEG C of heat 0.7Gcal.
Product separation and the energy regenerating that coal pyrolysis gas is carried out by the technique, are computed waste water ratio tradition ammonia spray work
Skill reduces 90%, and 85% heat can be recycled.
Embodiment 2
The utility model method is used for separation and the energy regenerating of coal pyrolysis gas, coal pyrolysis gas treating capacity is 60 tons/it is small
When, it is identical as the utility model process, including oil wash fractionating column, tower bottom circulating pump, tower bottom circulation heat exchanger, II carbolineum circulation
Pump, II carbolineum circulation heat exchanger, I carbolineum circulating pump, I carbolineum circulation heat exchanger, washing oil circulating pump, washing oil circulation heat exchanger, tower
Push up circulating pump, tower top circulation heat exchanger, II carbolineum stripper, I carbolineum stripper, washing oil stripper, condenser, storage tank, normal pressure
Knockout tower, reboiler, complete condenser.
Oil wash fractionation column pressure on top surface is 1.4bar, and tower reactor pressure is 1.8bar.Oil wash fractionating column totally 100 pieces of theoretical plates,
Side take-off enters washing oil stripper at theoretical plate 36, and side take-off enters I carbolineum stripper at theoretical plate 56, in theory
Side take-off enters II carbolineum stripper at plate 77, and tower top pump is produced at theoretical plate 15 and follows logistics, passes through tower bottom cycle heat exchange
Device carries out taking heat, and washing oil pump is produced at theoretical plate 36 and follows logistics, carries out taking heat by washing oil circulation heat exchanger, in theoretical plate 56
Extraction I carbolineum pump in place's follows logistics, carries out taking heat by I carbolineum circulation heat exchanger, and II carbolineum pump is produced at theoretical plate 77 and follows object
Stream, carries out taking heat by II carbolineum circulation heat exchanger, and column bottoms pump is produced at theoretical plate 91 and follows logistics, passes through tower bottom cycle heat exchange
Device carries out taking heat.Washing oil stripper, I carbolineum stripper and II carbolineum stripper have 15 pieces of theoretical plates.Reflux ratio is
0.0005。
Oil wash fractionator overhead temperature is 140 DEG C, and bottom temperature is 392 DEG C, and segregator temperature is 70 DEG C.
It is 346 DEG C that column bottoms pump, which follows extraction temperature, and it is 298 DEG C that II carbolineum pump, which follows extraction temperature, and I carbolineum pump follows extraction temperature and is
246 DEG C, it is 200 DEG C that washing oil pump, which follows extraction temperature, and tower top circulating temperature is 155 DEG C.
Atmospheric fractional tower has 40 pieces of theoretical plates, and it is tower top pressure 1.4bar at 20 pieces of theoretical plates, tower that carbolic oil, which produces position,
Kettle pressure is 1.5bar, reflux ratio 0.5.
Atmospheric fractional tower tower top temperature is 100 DEG C, and bottom temperature is 250 DEG C, and complete condenser temperature is 70 DEG C.
346 DEG C of heat 7.8Gcal can be recycled per hour, recycle 298 DEG C of heat 2.4Gcal, recycle 246 DEG C of heats
1.0Gcal recycles 200 DEG C of heat 0.9Gcal, recycles 155 DEG C of heat 0.7Gcal.
Product separation and the energy regenerating that coal pyrolysis gas is carried out by the technique, are computed waste water ratio tradition ammonia spray work
Skill reduces 90%, and 93% heat can be recycled.
Embodiment 3
The utility model method is used for separation and the energy regenerating of coal pyrolysis gas, coal pyrolysis gas treating capacity is 60 tons/it is small
When, it is identical as the utility model process, including oil wash fractionating column, tower bottom circulating pump, tower bottom circulation heat exchanger, II carbolineum circulation
Pump, II carbolineum circulation heat exchanger, I carbolineum circulating pump, I carbolineum circulation heat exchanger, washing oil circulating pump, washing oil circulation heat exchanger, tower
Push up circulating pump, tower top circulation heat exchanger, II carbolineum stripper, I carbolineum stripper, washing oil stripper, condenser, storage tank, normal pressure
Knockout tower, reboiler, complete condenser.
Oil wash fractionation column pressure on top surface is 1bar, and tower reactor pressure is 1.4bar.Oil wash fractionating column totally 75 pieces of theoretical plates, it is resonable
Enter washing oil stripper by side take-off at plate 30, side take-off enters I carbolineum stripper at theoretical plate 48, in theoretical plate
Side take-off enters II carbolineum stripper at 66, and tower top pump is produced at theoretical plate 12 and follows logistics, passes through tower bottom circulation heat exchanger
It carries out taking heat, washing oil pump is produced at theoretical plate 30 and follows logistics, carries out taking heat by washing oil circulation heat exchanger, at theoretical plate 48
Extraction I carbolineum pump follows logistics, carries out taking heat by I carbolineum circulation heat exchanger, and II carbolineum pump is produced at theoretical plate 66 and follows logistics,
It carries out taking heat by II carbolineum circulation heat exchanger, column bottoms pump is produced at theoretical plate 74 and follows logistics, passes through tower bottom circulation heat exchanger
It carries out taking heat.Washing oil stripper, I carbolineum stripper and II carbolineum stripper have 5 pieces of theoretical plates.Reflux ratio is 0.01.
Oil wash fractionator overhead temperature is 120 DEG C, and bottom temperature is 342 DEG C, and segregator temperature is 50 DEG C.
It is 316 DEG C that column bottoms pump, which follows extraction temperature, and it is 274 DEG C that II carbolineum pump, which follows extraction temperature, and I carbolineum pump follows extraction temperature and is
213 DEG C, it is 180 DEG C that washing oil pump, which follows extraction temperature, and tower top circulating temperature is 134 DEG C.
Atmospheric fractional tower has 25 pieces of theoretical plates, and it is tower top pressure 0.9bar at 7 pieces of theoretical plates, tower that carbolic oil, which produces position,
Kettle pressure is 1.2bar, reflux ratio 1.
Atmospheric fractional tower tower top temperature is 90 DEG C, and bottom temperature is 221 DEG C, and complete condenser temperature is 40 DEG C.
316 DEG C of heat 7.4Gcal can be recycled per hour, recycle 274 DEG C of heat 2.1Gcal, recycle 213 DEG C of heats
1.1Gcal recycles 180 DEG C of heat 1.0Gcal, recycles 134 DEG C of heat 0.9Gcal/h.
Product separation and the energy regenerating that coal pyrolysis gas is carried out by the technique, are computed waste water ratio tradition ammonia spray work
Skill reduces 90%, and 91% heat can be recycled.
Claims (4)
1. the equipment that a kind of separation of coal pyrolysis gas and energy regenerating integrate, it is characterised in that: followed including oil wash fractionating column, tower bottom
Ring pump, tower bottom circulation heat exchanger, II carbolineum circulating pump, II carbolineum circulation heat exchanger, I carbolineum circulating pump, I carbolineum cycle heat exchange
Device, washing oil circulating pump, washing oil circulation heat exchanger, tower top circulating pump, tower top circulation heat exchanger, II carbolineum stripper, I carbolineum stripping
Tower, washing oil stripper, condenser, storage tank, normal pressure knockout tower, reboiler, complete condenser；Pyrolysis oil gas enters oil wash fractionation from bottom
Tower；
Oil wash fractionating column and II carbolineum circulating pump are connected by returning to oil wash fractionation after II carbolineum circulation heat exchanger by pipeline
Tower；
Oil wash fractionating column and I carbolineum circulating pump are connected by returning to oil wash fractionating column after I carbolineum circulation heat exchanger by pipeline；
Oil wash fractionating column and washing oil circulating pump are connected by returning to oil wash fractionating column after washing oil circulation heat exchanger by pipeline；
Oil wash fractionating column and II carbolineum stripper are connected by pipeline, II carbolineum stripper tower bottom is produced equipped with logistics, tower overhead gas
Mutually return to oil wash fractionating column；
Oil wash fractionating column and I carbolineum stripper are connected by pipeline, I carbolineum stripper tower bottom is produced equipped with logistics, top gaseous phase
Return to oil wash fractionating column；
Oil wash fractionating column and washing oil stripper are connected by pipeline, washing oil stripper tower bottom is produced equipped with logistics, and top gaseous phase returns
Fractionating column is washed in oil return；
Oil wash fractionating column and condenser are connected by pipeline, storage tank is entered after condenser, storage tank is equipped with logistics extraction and portion
Return oil wash fractionation tower section is divided to enter normal pressure knockout tower；
Normal pressure knockout tower and reboiler and complete condenser are connected by pipeline, and is equipped with logistics extraction in tower top tower bottom survey line.
2. the equipment that the separation of coal pyrolysis gas according to claim 1 and energy regenerating integrate, it is characterised in that: the oil
Fractionating column is washed with 12-100 block theoretical plate, II carbolineum side take-off position is 6-77 block theoretical plate, I carbolineum side take-off position
Setting is 4-56 block theoretical plate, and washing oil side take-off position is 3-36 block reason theoretical plate.
3. the equipment that the separation of coal pyrolysis gas according to claim 1 and energy regenerating integrate, it is characterised in that: the oil
Washing fractionating column column bottoms pump and following extraction position is 8-91 block theoretical plate, and it is 6-77 block theoretical plate, I that II carbolineum pump, which follows extraction position,
It is 4-56 block theoretical plate that carbolineum pump, which follows extraction position, and it is 3-36 block theoretical plate that washing oil pump, which follows extraction position, and tower top pump, which follows, to be adopted
Out position is 3-15 block theoretical plate.
4. the equipment integrated according to the separation of coal pyrolysis gas described in claim 1 and energy regenerating, it is characterised in that: the oil wash
Fractionating column II carbolineum stripper number of theoretical plate is 2-15 block, and I carbolineum stripper number of theoretical plate is 2-15 block, and washing oil stripper is theoretical
Plate number 2-15 block.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820941950.8U CN208898797U (en) | 2018-06-19 | 2018-06-19 | A kind of equipment that the separation of coal pyrolysis gas is integrated with energy regenerating |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820941950.8U CN208898797U (en) | 2018-06-19 | 2018-06-19 | A kind of equipment that the separation of coal pyrolysis gas is integrated with energy regenerating |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208898797U true CN208898797U (en) | 2019-05-24 |
Family
ID=66566619
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820941950.8U Active CN208898797U (en) | 2018-06-19 | 2018-06-19 | A kind of equipment that the separation of coal pyrolysis gas is integrated with energy regenerating |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208898797U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115015464A (en) * | 2022-05-30 | 2022-09-06 | 天津大学 | Testing device and testing method for combustion characteristics and combustion mode of ammonia-mixed fuel |
-
2018
- 2018-06-19 CN CN201820941950.8U patent/CN208898797U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115015464A (en) * | 2022-05-30 | 2022-09-06 | 天津大学 | Testing device and testing method for combustion characteristics and combustion mode of ammonia-mixed fuel |
| CN115015464B (en) * | 2022-05-30 | 2023-10-27 | 天津大学 | Testing device and testing method for combustion characteristics and combustion modes of ammonia-mixed fuel |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101544913B (en) | Process and equipment for negative pressure benzene removal | |
| CN108101748B (en) | Four-tower three-effect methanol rectification energy-saving process method and device | |
| CN104817481B (en) | Technological method for recovering DMSO from DMSO aqueous solution | |
| CN102336432B (en) | Separation method for recovering olefin polymerization catalyst mother liquid | |
| CN104447480B (en) | A kind of nmp solvent continuous recovery method of polyphenylene sulfide process units | |
| CN208898797U (en) | A kind of equipment that the separation of coal pyrolysis gas is integrated with energy regenerating | |
| CN109355083A (en) | The technique and system of tri-mixed fractions are adopted in a kind of tar vacuum distillation | |
| CN106673289A (en) | Method and device for treating high-concentration organic phenol-containing coal gasification wastewater through enhanced extraction | |
| CN103614278A (en) | Device and method for processing molasses alcohol waste liquor | |
| CN106745421A (en) | A kind of multiple Intermediate Heat Exchanger rectification method treatment low concentration DMF waste water systems of band | |
| CN102199070A (en) | Tubular furnace method pressure-reduced debenzolization and distillation process | |
| CN101434510B (en) | Method and apparatus for recovering methyl chloride in organosilicon monomer synthesis | |
| CN102659508A (en) | Process method for vinyl chloride separation and refining | |
| CN108559530A (en) | A kind of method and apparatus that the separation of coal pyrolysis gas is integrated with energy regenerating | |
| CN105733647A (en) | Method for recovering liquefied petroleum gas from Fischer-Tropsch synthesis tail gas | |
| CN105779028B (en) | Raw coke oven gas heat and change based on washing rectifying produce the method recycled simultaneously | |
| CN100378048C (en) | Method of extracting, rectifying and separating aromatic hydrocarbons and extracting and rectifying apparatus | |
| CN108329193A (en) | One kind being used for coal-ethylene glycol industry ethylene glycol recovery process method and system | |
| CN108611104A (en) | A kind of method and apparatus that the separation of oil-sand pyrolysis oil gas is integrated with energy regenerating | |
| CN100339344C (en) | Styrene separation process | |
| CN108358754B (en) | Process method and system for separating ethanol, ethyl acetate and water mixture | |
| CN209276439U (en) | A kind of equipment that the separation of oil-sand pyrolysis oil gas is integrated with energy regenerating | |
| CN109355087A (en) | The step recyclable device and method of oil product in a kind of oil-containing dust and gas body | |
| CN101450909A (en) | Segregation and fractionation regeneration method of dimethylformamide as extracting solvent for cracking carbon 5 | |
| CN212152190U (en) | Coal tar three-tower continuous deep processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |