CN105969431A - Treatment system and method for pyrolysis oil and gas in new technique for producing calcium carbide - Google Patents
Treatment system and method for pyrolysis oil and gas in new technique for producing calcium carbide Download PDFInfo
- Publication number
- CN105969431A CN105969431A CN201610514959.6A CN201610514959A CN105969431A CN 105969431 A CN105969431 A CN 105969431A CN 201610514959 A CN201610514959 A CN 201610514959A CN 105969431 A CN105969431 A CN 105969431A
- Authority
- CN
- China
- Prior art keywords
- gas
- oil
- tar
- pyrolysis
- outlet
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
- C10K1/046—Reducing the tar content
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a treatment system and a treatment method for pyrolysis oil and gas in a new technique for producing calcium carbide. The treatment system comprises a calcium carbide production device, a quench tower and a flash tank, wherein the calcium carbide production device is provided with a binder inlet and a pyrolysis oil and gas outlet; the quench tower is provided with a pyrolysis oil and gas inlet and a heavy tar outlet; the flash tank is provided with a heavy tar inlet and a binder tar outlet; the pyrolysis oil and gas outlet is connected with the pyrolysis oil and gas inlet; the heavy tar outlet is connected with the heavy tar inlet; the binder tar outlet is connected with the binder inlet. The treatment method comprises the following steps of sending the pyrolysis oil and gas, which are generated by the calcium carbide production device, into the quench tower, and cooling the pyrolysis oil and gas under the spraying of cooling oil, so as to obtain heavy tar and preliminarily cooled oil and gas; flashing the heavy tar to remove light components, so as to subsequently obtain binder tar, and sending the binder tar into the calcium carbide production device to use the binder tar as a binder. By using the treatment system and the treatment method for the pyrolysis oil and gas in the new technique for producing the calcium carbide, the qualified binder tar is produced in the recovery process of the pyrolysis oil and gas; the binder tar is used as a molding effective binder component, thereby decreasing the cost of the binder.
Description
Technical field
The invention belongs to coal chemical technology is pyrolyzed processing system and the method for oil gas, specifically, be pyrolysis of coal and electricity
Stone produces during being coupled, and processes pyrolysis oil gas to obtain light Fuel and the system and method for binding agent tar.
Background technology
Carbide new technology refers to uniformly mix low order fine coal with Calx, is kneaded into pelletizing (> under binding agent effect
3mm), pelletizing first generates pyrolysis gas, tar and pyrolysis solid through heat accumulating type rotating bed pyrolysis, and pyrolysis solid material is by heated conveying
Carbide is produced to furnace of calcium carbide.This technique is a kind of effective way of coal sub-prime cascade utilization, carries out coupling aobvious with pyrolytic process
Write and reduce the energy consumption that carbide produces, and by-product coke oil and gas.
In carbide new technology, the pyrolysis temperature of pelletizing is 600～900 DEG C, and the tar heavy component of generation is the most, accounts for
More than 45%, typically tar is used as fuel, there is no and make full use of.Coking refining due to pyrolytic process with conventional coal
Burnt different, the tar viscosity that this process generates is relatively big, and in tar, mechanical admixture and toluene insolubles content are higher, conventional coking
In technique, the recovery method of raw coke oven gas is not suitable for this technique, so the feature according to new technology of needing badly proposes new pyrolysis oil gas
Processing method, makes pyrolysis oil gas obtain comprehensive utilization.
Summary of the invention
The defect that the tar that the present invention is directed to produce in existing production carbide new technology can not be fully utilized, proposes one
Produce processing system and the method being pyrolyzed oil gas in carbide new technology.
The present invention is the processing procedure being applied to be pyrolyzed in a kind of carbide production new technique oil gas, is to produce newly for carbide
The pyrolytic tar produced in technique is laid particular stress on, and major part is sold directly as heavy fuel, is not really achieved low-order coal sub-prime ladder
The deficiency of purpose that level utilizes and propose, in view of binding agent to be used in carbide new technology is used for the molding of carbide raw material, this
Invent the tar of the qualified viscosity of output in the removal process of pyrolysis oil gas, as fine coal and effective binding agent of Calx molding
Component, can significantly reduce binding agent cost；Binding agent tar is pyrolyzed in pyrolytic process again simultaneously, increases tar light oil
And pyrolysis gas, thus improve the economy of carbide production new technique.
The present invention is to be attained in that by following technical solution
A kind of produce the processing system being pyrolyzed oil gas in carbide new technology, including: calcium carbide production equipment, chilling tower and flash distillation
Tank；Described calcium carbide production equipment is provided with binding agent entrance, pyrolysis oil gas vent；Described chilling tower is provided with pyrolysis oil gas entrance, weight
Matter tar outlet；Described flash tank is provided with heavy tar entrance, binder coke oil export；Wherein, described pyrolysis oil gas vent is even
Connecing described pyrolysis oil gas entrance, the outlet of described heavy tar connects described heavy tar entrance, and described binder coke oil export is even
Connect described binding agent entrance.
Preferably, described chilling tower is provided with quench oil entrance, and the outlet of described heavy tar connects described urgency
Cold oil entrance.
Processing system of the present invention farther includes heavy tar storage tank, and described heavy tar storage tank is provided with entrance and exit,
Described entrance connects the outlet of described heavy tar, and described outlet connects described quench oil entrance.
Processing system of the present invention farther includes fractionating column, and described fractionating column is provided with feed(raw material)inlet；Described chilling tower is provided with
First cold oil gas vent, described flash tank is provided with light fraction outlet, and described just cold oil gas vent, described light fraction outlet connect described
Feed(raw material)inlet.
Processing system of the present invention also can farther include gas fractionation unit, and described gas fractionation unit is provided with gas and enters
Mouthful；Described calcium carbide production equipment is provided with offgas outlet, and described fractionating column is provided with pyrolysis gas outlet, described offgas outlet, described heat
Outlet of venting one's spleen connects described gas access.
Invention additionally discloses a kind of processing method producing and being pyrolyzed oil gas in carbide new technology, including:
Chilling: the pyrolysis oil pneumatic transmission that calcium carbide production equipment produces is entered chilling tower, cools down under cooling oil spray, obtains
Heavy tar and first cold oil gas；
Flash distillation or deep vacuum distillation: after heavy tar flash distillation or deep vacuum distillation are removed light components, obtain binding agent tar,
Binding agent tar feeding calcium carbide production equipment is made binding agent.
Preferably, described for part heavy tar is sent into chilling tower, spray as quench oil.
Processing method of the present invention can farther include fractionating step: the first cold oil gas that described chilling step obtained and described
The light components that flash steps obtains carries out fractional distillation, obtains pyrolysis gas and naphtha cut, diesel oil distillate and wax oil fraction.
Processing method of the present invention also can farther include gas separating step: is produced with calcium carbide production equipment by described pyrolysis gas
Raw tail gas is sent into gas fractionation unit and is separated, and obtains synthesis gas and fuel gas.
Wherein, the temperature of described quench oil is 40～90 DEG C；The temperature of described just cold oil gas is 360～385 DEG C.
The present invention is by the recovery to pyrolysis oil gas in carbide production new technique, it is thus achieved that gluing of carbide raw material molding
Knot agent tar, obtains light fuel fractions, such as naphtha cut, diesel oil distillate and wax oil fraction simultaneously.Employing heavy tar sprays
Drenching pyrolysis oil gas, the heavy tar cooled down obtains as carbide raw material molding after flashing off light components further
Binding agent, first cold tar and flash distillation light components enter rectifying column and obtain light fuel fractions, and calcium carbide tail gas and pyrolysis gas go
Gas separation unit, it is thus achieved that synthesis material or fuel.
Both can have been obtained suitable binding agent tar by the oil-gas recovery method of the present invention, directly reduce new technology core
The molding cost of heart technology, can make again to be again pyrolyzed as the part of binding agent tar, and then obtains more lightweight and evaporate
Divide and pyrolysis gas.
Accompanying drawing explanation
Pyrolysis oil gas processing system structural representation in the carbide production new technique that Fig. 1 provides for the present invention；
Pyrolysis oil gas disposal method flow schematic diagram in the carbide production new technique that Fig. 2 provides for the present invention.
Description of reference numerals
1, fine coal, 2, Calx, 3, former, 4, molding batch mixing, 5, revolving bed pyrolysis oven, 6, pyrolysis molding batch mixing, 7,
Pyrolysis oil gas, 8, furnace of calcium carbide, 9, carbide, 10, calcium carbide tail gas, 11, chilling tower, 12, heavy tar (cooling medium), 13, first cold
Oil gas, 14, heavy tar storage tank, 15, heavy tar, 16, flash vessel (vacuum distillation tower), 17, light component, 18, binder coke
Oil, 19, fractionating column, 20, pyrolysis gas, 21, gas trap, 22, synthesis gas (CO, H2), 23, fuel gas, 24, Petroleum evaporates
Point, 25, diesel oil distillate, 26, wax oil fraction.
Detailed description of the invention
The present invention discloses a kind of processing system and method producing and being pyrolyzed oil gas in carbide new technology.The present invention is in pyrolysis oil
The binding agent tar that in the removal process of gas, output is qualified, binding agent tar is as fine coal and effective binding agent group of Calx molding
Point can significantly reduce binding agent cost, binding agent tar is pyrolyzed in pyrolytic process again simultaneously, increase tar light oil and
Pyrolysis gas.
What the present invention provided produces the processing system being pyrolyzed oil gas in carbide new technology, including calcium carbide production equipment and pair
The aftertreatment device of product.
Specifically, calcium carbide production equipment includes that the forming unit being sequentially connected with, pyrolysis unit, carbide smelt unit.Powder
Coal and Calx are at the effect compacted under of binding agent, and molding batch mixing is admitted in revolving bed pyrolysis oven pyrolysis, produce pyrolysis oil gas and
Pyrolysis molding batch mixing；Pyrolysis molding batch mixing is admitted to furnace of calcium carbide heating, it is thus achieved that carbide.
The aftertreatment device of side-product includes quenching unit, flash evaporation unit.
Illustrating from the annexation of each unit, forming unit is provided with binding agent entrance, pyrolysis oil gas vent；Quenching unit
For chilling tower, chilling tower is provided with pyrolysis oil gas entrance, heavy tar outlet；Flash evaporation unit is flash tank, and flash tank is provided with heavy
Tar entrance, binder coke oil export；Wherein, pyrolysis oil gas vent connects pyrolysis oil gas entrance, and heavy tar outlet connects weight
Matter tar entrance, binder coke oil export connects binding agent entrance.It is to say, the pyrolysis oil gas quilt that revolving bed pyrolysis oven produces
Sending into quenching unit, obtain just cold oil gas and heavy tar, heavy tar gained tar after flash evaporation unit flash distillation is admitted to molding
Unit, for the binding agent of raw material.
It is light to separate in pyrolysis oil gas that the present invention can further include fractionation unit, gas separation unit etc.
Component carries out the equipment processed.The first cold oil gas that quenching unit obtains is sequentially sent to fractionation unit and gas separation unit do into
One step processes, and obtains light ends, becomes raw material and fuel gas.
The present invention collects the side-product pyrolysis oil gas producing carbide gained, processes and obtains the tar that viscosity is bigger, by this Jiao
Oil is sent in forming unit, serves as the binding agent of fine coal and Calx, had both solved what the big tar of viscosity can not be fully utilized
A difficult problem, simultaneously pyrolysis oil gas and calcium carbide tail gas respectively through subsequent cell process, in order to obtain naphtha cut, diesel oil distillate,
Wax oil fraction, binding agent tar, synthesis gas and fuel gas, each fraction hydrotreating can obtain light Fuel oil product further.
Below in conjunction with the embodiment shown in Fig. 1, Fig. 2, the present invention will be further described, but embodiment the most therefore and
Limit the range of the present invention.
As it is shown in figure 1, the processing system being pyrolyzed oil gas in production carbide new technology includes forming unit, pyrolysis unit, electricity
Stone smelts unit, quenching unit, flash evaporation unit, fractionation unit, gas separation unit.
Described forming unit includes former 3.Former 3 is provided with fine coal entrance, lime inlet and binding agent tar
Suction line, molding batch mixing export；Fine coal 1, Calx 2 are put into former 3 by fine coal entrance, lime inlet respectively.Bonding
Agent tar 18 is imported former 3 by binder coke oil-in pipeline.Fine coal 1, Calx 2 are in the effect of binding agent tar 18
Under, it is pressed into molding batch mixing 4, the outlet of molding batch mixing discharges former 3.
Described pyrolysis unit includes revolving bed pyrolysis oven 5.Revolving bed pyrolysis oven 5 is provided with pyrolysis molding batch mixing outlet, pyrolysis
Oil gas vent, described revolving bed pyrolysis oven 5 is connected with former 3.Molding batch mixing 4 is pyrolyzed in revolving bed pyrolysis oven 5, obtains
Pyrolysis molding batch mixing 6 and pyrolysis oil gas 7, be discharged revolving bed pyrolysis by pyrolysis molding batch mixing outlet, pyrolysis oil gas vent respectively
Stove 5.
Described carbide is smelted unit and is included furnace of calcium carbide 8.The outlet of furnace of calcium carbide 8 carbide and calcium carbide tail gas export 10, and furnace of calcium carbide 8 leads to
Cross the outlet of pyrolysis molding batch mixing to be connected with revolving bed pyrolysis oven 5.Pyrolysis molding batch mixing 6 heats in furnace of calcium carbide 8, obtains carbide 9
With calcium carbide tail gas 10.
Described quenching unit includes chilling tower 11.Described chilling tower 11 bottom arranges pyrolysis oil and gas import, at the beginning of top is arranged
Cold oil gas vent, top arranges quench oil import.Pyrolysis oil and gas import is connected with the pyrolysis oil gas vent of revolving bed by pipeline.
The bottom of chilling tower 11 arranges heavy tar outlet, is connected with heavy tar storage tank 14.Pyrolysis oil gas 7 is by the pyrolysis oil of tower bottom
Gas import enters chilling tower 11, during moving up, runs into the cooling medium 12 that tower internal upper part sprays and cools down.Not by
The gas of cooling is first cold oil gas 13, the first cold oil gas vent of top of tower discharge.Cooled liquid component is heavy tar,
Discharge to flash tank from heavy tar outlet.
Preferably, present invention additionally comprises heavy tar storage tank 14, heavy tar storage tank is provided with entrance and goes out
Mouthful, entrance connect chilling tower 11 top heavy tar outlet, outlet connect flash tank quench oil entrance.Heavy tar stores up
Part heavy tar in tank 14 is sent into chilling tower 11 by the quench oil import on chilling tower 11 top, is used as pyrolysis oil
The cooling medium 12 of gas.Heavy tar collected by heavy tar storage tank 14, and part is gone flash distillation as cooling medium, part, made operation
It is easily achieved.
Described flash evaporation unit includes flash tank 16.Flash tank 16 bottom arranges heavy tar import, by pipeline and heavy
Tar storage tank 14 is connected, and top arranges light fraction outlet, is connected with fractionating column 19 by pipeline, and bottom arranges binding agent tar and goes out
Mouthful, it is connected with former 3 by pipeline.Heavy tar, in flash tank 16 flash distillation, obtains the light component 17 of gaseous state and has relatively
The binding agent tar 18 of good viscosity.Binding agent tar 18 is admitted to former 3 by binder coke oil export and does binding agent use.
Light component 17 is entered fractionating column 19 by light fraction outlet.
Described fractionation unit includes fractionating column 19.Fractionating column 19 bottom arranges charging aperture, by pipeline and chilling tower 11 phase
Even, top arranges pyrolysis gas outlet, sets gradually naphtha cut lateral line withdrawal function mouth, diesel oil distillate lateral line withdrawal function under upper
Mouthful, bottom arranges wax oil fraction outlet port.The light component 17 that the first cold oil gas produced by chilling tower 11 and flash tank 16 produce is made
For raw material, charging aperture entering fractionating column 19, obtain pyrolysis gas 20, naphtha cut 24 after fractional distillation, diesel oil distillate 25, wax oil evaporate
Divide 26, discharge fractionating column 19 respectively.
Described gas separation unit includes gas trap 21.Described gas trap 21 arranges syngas outlet, fuel
Gas exports.Air inlet is connected with calcium carbide stove exhaust outlet and fractionating column pyrolysis gas outlet by pipeline.Calcium carbide stove exhaust 10 and heat
Vent one's spleen and 20 in gas trap 21, be separated into synthesis gas 22 (composition is CO, H2), fuel gas 23.
Invention additionally discloses a kind of processing method produced in carbide new technology, processing method includes:
Chilling: the pyrolysis oil pneumatic transmission that calcium carbide production equipment produces is entered chilling tower, cools down under cooling oil spray, obtains
Heavy tar and first cold oil gas；
Flash distillation: obtain binding agent tar after heavy tar flash distillation is removed light components, binding agent tar is sent into carbide
Process units makees binding agent.
Fig. 2 is shown that using above-mentioned processing system to implement to produce the processing method in carbide new technology, for the present invention's
One embodiment, during producing in carbide new technology, pyrolysis feed produces pyrolysis oil gas, processes the concrete mistake of pyrolysis oil gas
Journey comprises the following steps:
(1) the pyrolysis oil gas of spin rotated bed pyrolysis oven enters chilling tower, utilizes heavy tar as cooling in chilling tower
Medium, by the heavy tar in spraying cooling mode pyrolysis oil gas；
(2) heavy tar enters heavy tar storage tank, and a part returns chilling tower and makees cooling medium, a part of heavy tar
Entering flash tank, obtain binding agent tar after flash tank removes light components, binding agent tar is delivered to forming unit and glues
Knot agent；
(3) fractional distillation is entered together with the light components that the pyrolysis oil gas (first cold oil gas) that chilling tower is not cooled comes with flash tank
Tower, it is thus achieved that pyrolysis gas, each tarry distillate (naphtha cut, diesel oil distillate, wax oil fraction)；
(4) pyrolysis gas enters gas separation unit together with calcium carbide tail gas, isolates synthesis gas (CO, H2) former as synthesis
Material or hydrogen feedstock, other component gas can be as fuel gas.
In the present invention, the temperature of revolving bed pyrolysis oil gas is 600～900 DEG C, as the temperature of the heavy tar of cooling medium
Being 40～90 DEG C, pyrolysis oil gas is cooled to 360～385 DEG C, it is thus achieved that first cold oil gas.Flash temperature is 280～350 DEG C.
It should be noted that the heavy tar flash tank 16 in above-mentioned Fig. 1 embodiment can also use vacuum distillation tower
Replacing, correspondingly, the flash steps deep vacuum distillation in Fig. 2 replaces.Decompression distillation deep drawing final temperature 540～565 DEG C, flash distillation and
The purpose of deep vacuum distillation is to reduce the light components in heavy tar, it is ensured that the index of binding agent tar.
Adding the amount of binding agent tar in the present invention in fine coal and Calx forming process is 2～8% (to account for bonding gross mass
Percent).
Providing below specific embodiment, the present invention will be described in detail.
Embodiment in the present invention uses somewhere brown coal to be carbon back raw material, and brown coal main character is shown in Table 1, and quick lime is calcio
Raw material, wherein CaO content is 94% (mass fraction).
Table 1 brown coal main character
Embodiment 1
The powdery brown coal of drying, Calx enter former, be stirring evenly and then adding into 6% binding agent tar and its
Its binder component (clay, waterglass etc.) molding on roller press briquetting equipment, molding batch mixing enters revolving bed pyrolysis oven to be carried out
Pyrolysis, molding batch mixing after pyrolysis enter furnace of calcium carbide generate carbide and calcium carbide tail gas, pyrolysis oil gas and calcium carbide tail gas respectively through
Subsequent cell processes, in order to obtain naphtha cut, diesel oil distillate, wax oil fraction, synthesis gas and fuel gas.
Pyrolysis oil gas and the processing method of calcium carbide tail gas, specifically includes following steps:
(1) the pyrolysis oil gas of spin rotated bed pyrolysis oven 750 DEG C enters chilling tower, and the heavy utilizing 60 DEG C in chilling tower is burnt
Oil is as cooling medium, and by the heavy tar in spraying cooling mode pyrolysis oil gas, not cooled pyrolysis oil gas is (just
Cold oil gas) it is cooled to 370 DEG C；
(2) heavy tar enters heavy tar storage tank, and a part returns chilling tower and does cooling medium, a part of heavy tar
Entering flash tank, obtain binding agent tar after flash distillation removes light components at 320 DEG C, binding agent tar is delivered to forming unit
Make binding agent；
(3) fractional distillation is entered together with the light components that the pyrolysis oil gas (first cold oil gas) that chilling tower is not cooled comes with flash tank
Tower, it is thus achieved that pyrolysis gas, each tarry distillate (naphtha cut, diesel oil distillate, wax oil fraction)；
(4) pyrolysis gas enters gas separation unit together with calcium carbide tail gas, isolates synthesis gas (CO, H2) and other component
Gas is as fuel gas.
Reaction primary product composition and character are shown in Table 2.
Embodiment 2
The powdery brown coal of drying, Calx enter former, be stirring evenly and then adding into 4% binding agent tar and its
Its binder component (clay, waterglass etc., with embodiment 1) molding on roller press briquetting equipment, molding batch mixing enters revolving bed
Pyrolysis oven is pyrolyzed, and the molding batch mixing after pyrolysis enters furnace of calcium carbide and generates carbide and calcium carbide tail gas, pyrolysis oil gas and carbide tail
Gas processes respectively through subsequent cell, in order to obtain naphtha cut, diesel oil distillate, wax oil fraction, synthesis gas and fuel gas.
Pyrolysis oil gas and the processing method of calcium carbide tail gas, specifically includes following steps:
(1) the pyrolysis oil gas of spin rotated bed pyrolysis oven 800 DEG C enters chilling tower, and the heavy utilizing 40 DEG C in chilling tower is burnt
Oil is as cooling medium, and by the heavy tar in spraying cooling mode pyrolysis oil gas, not cooled pyrolysis oil gas is (just
Cold oil gas) it is cooled to 385 DEG C；
(2) heavy tar enters heavy tar storage tank, and a part returns chilling tower and does cooling medium, a part of heavy tar
Entering vacuum distillation tower, vacuum distillation tower deep drawing temperature is 550 DEG C, it is thus achieved that binding agent tar, and binding agent tar is delivered to molding
Unit makees binding agent；
(3) fractional distillation is entered together with the light components that the pyrolysis oil gas (first cold oil gas) that chilling tower is not cooled comes with flash tank
Tower, it is thus achieved that pyrolysis gas, each tarry distillate (naphtha cut, diesel oil distillate, wax oil fraction)；
(4) pyrolysis gas enters gas separation unit together with calcium carbide tail gas, isolates synthesis gas (CO, H2) and other component
Gas is as fuel gas.
Reaction primary product composition and character are shown in Table 2.
Embodiment 3
The powdery brown coal of drying, Calx enter former, be stirring evenly and then adding into 2% binding agent tar and its
Its binder component (clay, waterglass etc., with embodiment 1) molding on roller press briquetting equipment, molding batch mixing enters revolving bed
Pyrolysis oven is pyrolyzed, and the molding batch mixing after pyrolysis enters furnace of calcium carbide and generates carbide and calcium carbide tail gas, pyrolysis oil gas and carbide tail
Gas processes respectively through subsequent cell, in order to obtain naphtha cut, diesel oil distillate, wax oil fraction, synthesis gas and fuel gas.
Pyrolysis oil gas and the processing method of calcium carbide tail gas, specifically includes following steps:
(1) the pyrolysis oil gas of spin rotated bed pyrolysis oven 600 DEG C enters chilling tower, and the heavy utilizing 90 DEG C in chilling tower is burnt
Oil is as cooling medium, and by the heavy tar in spraying cooling mode pyrolysis oil gas, not cooled pyrolysis oil gas is (just
Cold oil gas) it is cooled to 385 DEG C；
(2) heavy tar enters heavy tar storage tank, and a part returns chilling tower and does cooling medium, a part of heavy tar
Entering flash tank, obtain binding agent tar after flash distillation removes light components at 350 DEG C, binding agent tar is delivered to forming unit
Make binding agent；
(3) fractional distillation is entered together with the light components that the pyrolysis oil gas (first cold oil gas) that chilling tower is not cooled comes with flash tank
Tower, it is thus achieved that pyrolysis gas, each tarry distillate (naphtha cut, diesel oil distillate, wax oil fraction)；
(4) pyrolysis gas enters gas separation unit together with calcium carbide tail gas, isolates synthesis gas (CO, H2) and other component
Gas is as fuel gas.
Reaction primary product composition and character are shown in Table 2.
Embodiment 4
The powdery brown coal of drying, Calx enter former, be stirring evenly and then adding into 7% binding agent tar and its
Its binder component (clay, waterglass etc., with embodiment 1) molding on roller press briquetting equipment, molding batch mixing enters revolving bed
Pyrolysis oven is pyrolyzed, and the molding batch mixing after pyrolysis enters furnace of calcium carbide and generates carbide and calcium carbide tail gas, pyrolysis oil gas and carbide tail
Gas processes respectively through subsequent cell, in order to obtain naphtha cut, diesel oil distillate, wax oil fraction, synthesis gas and fuel gas.
Pyrolysis oil gas and the processing method of calcium carbide tail gas, specifically includes following steps:
(1) the pyrolysis oil gas of spin rotated bed pyrolysis oven 700 DEG C enters chilling tower, and the heavy utilizing 80 DEG C in chilling tower is burnt
Oil is as cooling medium, and by the heavy tar in spraying cooling mode pyrolysis oil gas, not cooled pyrolysis oil gas is (just
Cold oil gas) it is cooled to 360 DEG C；
(2) heavy tar enters heavy tar storage tank, and a part returns chilling tower and does cooling medium, a part of heavy tar
Entering flash tank, obtain binding agent tar after flash distillation removes light components at 280 DEG C, binding agent tar is delivered to forming unit
Make binding agent；
(3) fractional distillation is entered together with the light components that the pyrolysis oil gas (first cold oil gas) that chilling tower is not cooled comes with flash tank
Tower, it is thus achieved that pyrolysis gas, each tarry distillate (naphtha cut, diesel oil distillate, wax oil fraction)；
(4) pyrolysis gas enters gas separation unit together with calcium carbide tail gas, isolates synthesis gas (CO, H2) and other component
Gas is as fuel gas.
Reaction primary product composition and character are shown in Table 2.
Embodiment 5
The powdery brown coal of drying, Calx enter former, be stirring evenly and then adding into 3% binding agent tar and its
Its binder component (clay, waterglass etc., with embodiment 1) molding on roller press briquetting equipment, molding batch mixing enters revolving bed
Pyrolysis oven is pyrolyzed, and the molding batch mixing after pyrolysis enters furnace of calcium carbide and generates carbide and calcium carbide tail gas, pyrolysis oil gas and carbide tail
Gas processes respectively through subsequent cell, in order to obtain naphtha cut, diesel oil distillate, wax oil fraction, synthesis gas and fuel gas.
Pyrolysis oil gas and the processing method of calcium carbide tail gas, specifically includes following steps:
(1) the pyrolysis oil gas of spin rotated bed pyrolysis oven 900 DEG C enters chilling tower, and the heavy utilizing 90 DEG C in chilling tower is burnt
Oil is as cooling medium, and by the heavy tar in spraying cooling mode pyrolysis oil gas, not cooled pyrolysis oil gas is (just
Cold oil gas) it is cooled to 370 DEG C；
(2) heavy tar enters heavy tar storage tank, and a part returns chilling tower and does cooling medium, a part of heavy tar
Entering vacuum distillation tower, vacuum distillation tower deep drawing temperature is 540 DEG C, it is thus achieved that binding agent tar, and binding agent tar is delivered to molding
Unit makees binding agent；
(3) fractional distillation is entered together with the light components that the pyrolysis oil gas (first cold oil gas) that chilling tower is not cooled comes with flash tank
Tower, it is thus achieved that pyrolysis gas, each tarry distillate (naphtha cut, diesel oil distillate, wax oil fraction)；
(4) pyrolysis gas enters gas separation unit together with calcium carbide tail gas, isolates synthesis gas (CO, H2) and other component
Gas is as fuel gas.
Reaction primary product composition and character are shown in Table 2.
Embodiment 6
The powdery brown coal of drying, Calx enter former, be stirring evenly and then adding into 8% binding agent tar and its
Its binder component (clay, waterglass etc., with embodiment 1) molding on roller press briquetting equipment, molding batch mixing enters revolving bed
Pyrolysis oven is pyrolyzed, and the molding batch mixing after pyrolysis enters furnace of calcium carbide and generates carbide and calcium carbide tail gas, pyrolysis oil gas and carbide tail
Gas processes respectively through subsequent cell, in order to obtain naphtha cut, diesel oil distillate, wax oil fraction, synthesis gas and fuel gas.
Pyrolysis oil gas and the processing method of calcium carbide tail gas, specifically includes following steps:
(1) the pyrolysis oil gas of spin rotated bed pyrolysis oven 650 DEG C enters chilling tower, and the heavy utilizing 50 DEG C in chilling tower is burnt
Oil is as cooling medium, and by the heavy tar in spraying cooling mode pyrolysis oil gas, not cooled pyrolysis oil gas is (just
Cold oil gas) it is cooled to 360 DEG C；
(2) heavy tar enters heavy tar storage tank, and a part returns chilling tower and does cooling medium, a part of heavy tar
Entering vacuum distillation tower, vacuum distillation tower deep drawing temperature is 565 DEG C, it is thus achieved that binding agent tar, and binding agent tar is delivered to molding
Unit makees binding agent；
(3) fractional distillation is entered together with the light components that the pyrolysis oil gas (first cold oil gas) that chilling tower is not cooled comes with flash tank
Tower, it is thus achieved that pyrolysis gas, each tarry distillate (naphtha cut, diesel oil distillate, wax oil fraction)；
(4) pyrolysis gas enters gas separation unit together with calcium carbide tail gas, isolates synthesis gas (CO, H2) and other component
Gas is as fuel gas.
Reaction primary product composition and character are shown in Table 2.
Table 2 product mainly comprises and character
Oil vapor treatment method involved in the present invention is particularly suited for producing acquisition binding agent tar in carbide new technology,
It is also applied for oil shale, bitumen, oil-sand etc. and needs to obtain the pyrolytic process of binder pitch.
Coal powder formation in carbide new technology is one of core procedure of technique, and the method passes through technique by-product tar own
Binding agent, both can meet forming requirements, can significantly reduce again the cost of outsourcing binding agent, and as the heavy tar of binding agent
Again it is pyrolyzed and can obtain light components and gas, in order to promote the economy of carbide new technology.
What present disclosure was touched upon is exemplary embodiment, at the protection domain defined without departing from claims
In the case of, each embodiment of the present invention can be made various changes and modifications.Therefore, described embodiment is intended to contain
All this type of that lid falls in the protection domain of appended claims changes, revises and deform.Additionally, institute unless the context
Outside finger, the word occurred in the singular includes plural form, and vice versa.It addition, unless stated otherwise, then any embodiment
All or part of can in conjunction with any other embodiments all or part of use.
Claims (10)
1. one kind produces the processing system being pyrolyzed oil gas in carbide new technology, it is characterised in that including: calcium carbide production equipment, urgency
Cold tower and flash tank；
Described calcium carbide production equipment is provided with binding agent entrance, pyrolysis oil gas vent；
Described chilling tower is provided with pyrolysis oil gas entrance, heavy tar outlet；
Described flash tank is provided with heavy tar entrance, binder coke oil export；
Wherein, described pyrolysis oil gas vent connects described pyrolysis oil gas entrance, and it is burnt that the outlet of described heavy tar connects described heavy
Oil-in, described binder coke oil export connects described binding agent entrance.
2. processing system as claimed in claim 1, it is characterised in that described chilling tower is provided with quench oil entrance, described heavy
Tar outlet connects described quench oil entrance.
3. processing system as claimed in claim 2, it is characterised in that farther including heavy tar storage tank, described heavy is burnt
Oil tank is provided with entrance and exit, and described entrance connects the outlet of described heavy tar, and described outlet connects described quench oil entrance.
4. processing system as claimed in claim 2, it is characterised in that farther including fractionating column, described fractionating column is provided with former
Material entrance；Described chilling tower is provided with just cold oil gas vent, and described flash tank is provided with light fraction outlet, described just cold oil gas vent,
Described light fraction outlet connects described feed(raw material)inlet.
5. processing system as claimed in claim 4, it is characterised in that farther including gas fractionation unit, described gas divides
It is provided with gas access from device；Described calcium carbide production equipment is provided with offgas outlet, and described fractionating column is provided with pyrolysis gas outlet, described
Offgas outlet, described pyrolysis gas outlet connect described gas access.
6. one kind produces the processing method being pyrolyzed oil gas in carbide new technology, it is characterised in that the treating method comprises:
Chilling: the pyrolysis oil pneumatic transmission that calcium carbide production equipment produces is entered chilling tower, cools down under cooling oil spray, obtains heavy
Tar and first cold oil gas；
Flash distillation or deep vacuum distillation: obtain binding agent tar after heavy tar flash distillation or deep vacuum distillation are removed light components, will be viscous
Knot agent tar is sent into calcium carbide production equipment and is made binding agent.
7. processing method as claimed in claim 6, it is characterised in that described for part heavy tar is sent into chilling tower, as
Quench oil sprays.
8. processing method as claimed in claim 7, it is characterised in that farther include fractionating step: by described chilling step
The light components that the first cold oil gas obtained and described flash distillation or deep vacuum distillation step obtain carries out fractional distillation, obtains pyrolysis gas and stone brain
Oil distillate, diesel oil distillate and wax oil fraction.
9. processing method as claimed in claim 8, it is characterised in that farther include gas separating step: by described pyrolysis
The tail gas that gas produces with calcium carbide production equipment is sent into gas fractionation unit and is separated, and obtains synthesis gas and fuel gas.
10. processing method as claimed in claim 9, it is characterised in that the temperature of described quench oil is 40～90 DEG C；At the beginning of described
The temperature of cold oil gas is 360～385 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610514959.6A CN105969431A (en) | 2016-07-01 | 2016-07-01 | Treatment system and method for pyrolysis oil and gas in new technique for producing calcium carbide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610514959.6A CN105969431A (en) | 2016-07-01 | 2016-07-01 | Treatment system and method for pyrolysis oil and gas in new technique for producing calcium carbide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105969431A true CN105969431A (en) | 2016-09-28 |
Family
ID=56955171
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610514959.6A Pending CN105969431A (en) | 2016-07-01 | 2016-07-01 | Treatment system and method for pyrolysis oil and gas in new technique for producing calcium carbide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105969431A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055539A (en) * | 2017-05-31 | 2017-08-18 | 神雾环保技术股份有限公司 | A kind of system for producing calcium carbide and method for removing magnesia |
| CN109355087A (en) * | 2018-11-21 | 2019-02-19 | 陕西延长石油（集团）有限责任公司 | The step recyclable device and method of oil product in a kind of oil-containing dust and gas body |
| CN109971513A (en) * | 2019-03-25 | 2019-07-05 | 武汉科技大学 | The multistage cooling technique and device of coal oven dithio-gas |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202450059U (en) * | 2012-03-09 | 2012-09-26 | 湖南大唐先一科技有限公司 | High-temperature gas purifying and recovering unit |
| US20130047509A1 (en) * | 2008-07-16 | 2013-02-28 | Kellogg Brown & Root Llc | Systems And Methods For Producing Substitute Natural Gas |
| CN104556036A (en) * | 2014-12-26 | 2015-04-29 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing solid calcium carbide |
| CN104803819A (en) * | 2015-05-15 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and system for producing ethylene by utilizing pulverized coal |
| CN205838933U (en) * | 2016-07-01 | 2016-12-28 | 北京神雾环境能源科技集团股份有限公司 | A kind of produce the processing system being pyrolyzed oil gas in carbide new technology |
-
2016
- 2016-07-01 CN CN201610514959.6A patent/CN105969431A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130047509A1 (en) * | 2008-07-16 | 2013-02-28 | Kellogg Brown & Root Llc | Systems And Methods For Producing Substitute Natural Gas |
| CN202450059U (en) * | 2012-03-09 | 2012-09-26 | 湖南大唐先一科技有限公司 | High-temperature gas purifying and recovering unit |
| CN104556036A (en) * | 2014-12-26 | 2015-04-29 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing solid calcium carbide |
| CN104803819A (en) * | 2015-05-15 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and system for producing ethylene by utilizing pulverized coal |
| CN205838933U (en) * | 2016-07-01 | 2016-12-28 | 北京神雾环境能源科技集团股份有限公司 | A kind of produce the processing system being pyrolyzed oil gas in carbide new technology |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107055539A (en) * | 2017-05-31 | 2017-08-18 | 神雾环保技术股份有限公司 | A kind of system for producing calcium carbide and method for removing magnesia |
| CN109355087A (en) * | 2018-11-21 | 2019-02-19 | 陕西延长石油（集团）有限责任公司 | The step recyclable device and method of oil product in a kind of oil-containing dust and gas body |
| CN109355087B (en) * | 2018-11-21 | 2021-01-15 | 陕西延长石油（集团）有限责任公司 | Step recovery device and method for oil product in gas containing oil dust |
| CN109971513A (en) * | 2019-03-25 | 2019-07-05 | 武汉科技大学 | The multistage cooling technique and device of coal oven dithio-gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107177378B (en) | The supercritical extract of heavy oil feedstock and the combined system of floating bed hydrogenation and method | |
| CN103275744B (en) | Asphalt substance separated from direct coal liquefaction residues and method and application thereof | |
| CN101962561B (en) | Extraction method of direct coal liquefaction residues and application of extracts | |
| CN106433775B (en) | A kind of kerosene is total to smelting method and its device | |
| CN103436280B (en) | Coal directly-liquefied residue is utilized to prepare the method for coke | |
| RU2686152C1 (en) | Method of producing oil needle coke | |
| CN105778968A (en) | Method for preparing impregnating pitch, impregnating pitch and application thereof | |
| CN105969431A (en) | Treatment system and method for pyrolysis oil and gas in new technique for producing calcium carbide | |
| CN103723728A (en) | Activated carbon and method for preparing activated carbon from coal-directly liquefied residue | |
| CN104232129B (en) | A kind of method that organic waste and coal copyrolysis produce semicoke and tar | |
| CN101602953A (en) | The purification system of straw quick thermal cracking products | |
| CN103254933B (en) | Method for separating liquefied heavy oil and asphalt substances from direct coal liquefaction residues | |
| CN103113909A (en) | Method for modifying and tackifying low-rank coals | |
| CN103756703A (en) | Modified asphalt, method for preparing modified asphalt by using direct liquefied coal residue in normal pressure continuous mode and application of modified coal residue | |
| CN101575537B (en) | Process for producing light and heavy fuel oil and high-quality asphalt by hydrogenating coal tar at medium and low temperature | |
| CN205838933U (en) | A kind of produce the processing system being pyrolyzed oil gas in carbide new technology | |
| CN105861014A (en) | Method for preparing impregnation pitch using direct coal liquefaction residue, impregnation pitch and application thereof | |
| CN105936834A (en) | Combined system and method for processing oil gas generated by pyrolysis of low rank coal | |
| CN109111950A (en) | The method of full fraction hydrogenation of tar production liquid fuel | |
| CN106281449B (en) | A kind of method and system of coal tar production light Fuel and needle coke | |
| CN106883871A (en) | A kind of production method of needle-shape coke raw material | |
| CN105713647B (en) | A kind of utilization coal tar maximization prepares the method and device of carbolic oil and diesel oil | |
| CN105950227A (en) | Treatment system and method for pyrolyzed oil gas | |
| CN206051957U (en) | A kind of processing system of pyrolysis oil gas | |
| CN103275758B (en) | Heavy oil full-fraction hydrotreatment method and system thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant after: Shenwu science and technology group Limited by Share Ltd Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
|
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20160928 |