CN1259391C - Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system - Google Patents
Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system Download PDFInfo
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- CN1259391C CN1259391C CN 200310100482 CN200310100482A CN1259391C CN 1259391 C CN1259391 C CN 1259391C CN 200310100482 CN200310100482 CN 200310100482 CN 200310100482 A CN200310100482 A CN 200310100482A CN 1259391 C CN1259391 C CN 1259391C
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Abstract
The present invention relates to a method and a system for cracking heavy hydrocarbons to prepare low-carbon olefin. The system uses an obsoleteblast furnace in an iron and steel enterprise as a main body and the blast furnace is reformed to a cracking and gasifying furnace by adding the outlet and the inlet of raw materials and products. The method comprises the steps that a cracking process and a heat supply process are integrated in the same reactor; coke used as a heat source and a heat carrier is filled into the reactor; oxygen is filled into a burning zone at the lower part of the reactor for burning and cracking raw materials and steam are sprayed into a cracking and gasifying zone at the middle part of the reactor to crack hydrocarbons and gasify coke; gas products are led out from a gasification completion zone at the upper part of the reactor and are compressed and separated in a cold box to obtain synthetic gas, low-carbon olefin, etc. after being cooled and purified; alkane is cracked again in the reactor and coke consumed in the reaction is supplemented by coke formations cracked by the heavy hydrocarbons. Compared with a conventional heavy hydrocarbon cracking technology, the method can use heavier hydrocarbons as raw materials and does not worry about the problem of coking formations, and outlet gas has the ethene content of more than 10% and is mixed to prepare the synthetic gas.
Description
Technical field
The present invention relates to a kind of cracking and produce the method for low-carbon alkene, particularly relate to the direct cracking of a kind of employing heavy hydrocarbon, producing ethene, and co-production synthesis gas (CO+H
2) and the heavy hydrocarbon cracking of low-carbon alkenes such as propylene, butylene produce the method and the pyrolysis gasification furnace system of low-carbon alkene.
Background technology
The tube furnace high-temperature cracking method is the main stream approach of ethylene production, and the ethene that adopts this method production at present in the world is up to more than 99% of ethene ultimate production.The topmost processing parameter of tube furnace high-temperature cracking method is high temperature, short residence time(SRT) and low hydrocarbon partial pressure, cracking stock comprises light petroleum hydrocarbons such as petroleum naphtha, solar oil, liquefied petroleum gas (LPG), ethane, is topmost raw material sources with petroleum naphtha and ethane again wherein.According to statistics, the ethene that these two kinds of raw materials are originated from the whole world surpasses 75% of ethene ultimate production, as document [1] Cui Jingyi. ethylene raw development trend and optimize suggestion. the economic .2001 of petrochemical technology, 17 (6). in introduced.Maintaining sustained and rapid growth of the market requirement of China's ethene and throughput makes the imbalance between supply and demand of nervous originally light hydrocarbon raw material outstanding day by day.
An aspect of China's ongoing effort for many years is to wish the cracking stock of heavy hydrocarbon (crude oil, heavy oil, residual oil or polyolefine plastic waste etc.) as ethylene production.The heavy hydrocarbon cracking needs higher cracking temperature, and tube furnace makes it to be difficult to become the cracking apparatus of heavy hydrocarbon because of there being the difficulty of furnace tube material and operating aspect.The boiler tube creep-resistant property reduces the work-ing life that will shorten boiler tube under the high temperature, and is easier in the coking of boiler tube inwall during the heavy hydrocarbon cracking, increased the heat transfer and the resistance to flow of boiler tube.
Non-tube furnace heavy hydrocarbon cracking technology was once studied by China, and typical case wherein is represented as regenerative furnace pyrolysis technology and sand cracking technology.The regenerative furnace pyrolysis method is because efficiency of utilization is low, and environmental pollution is big, and the high many-sided reason of energy consumption lacks competitive economically; Sand oven process complicated operation, equipment attrition is serious, heat recovery efficiency is low, antiquated sand is difficult to handle; These two kinds of technologies are all further developed in recent years and are gone out of use gradually, as document [2]: Ceng Qingquan. ethene. and chemical encyclopedia (18). Beijing: the .1998.866-867 of Chemical Industry Press.
The total oxygen blast furnace has in same reactor as ironmaking equipment and reacts and heat supply, and the characteristics that thermo-efficiency is high, the chamber design of blast furnace make it to bear high temperature, do not have the anxiety of coking and blocking pipeline again.Increase the entry and exit of raw material and product in the appropriate location of blast furnace, can transform as and can satisfy the pyrolysis gasification stove that the low-carbon alkene processing requirement is produced in the heavy hydrocarbon cracking.The coking that the heavy hydrocarbon cracking is loose, oxygen inflatable combustion heat supplying, co-production synthesis gas (CO+H simultaneously
2).Along with the process that the Iron And Steel Industry blast furnace maximizes, will there be many modern retired blast furnaces in China, produce the pyrolysis gasification stove of low-carbon alkene and co-production synthesis gas as it being transform as the heavy hydrocarbon cracking, and the iron and steel enterprise of the middle and small scale of can yet be regarded as provides an outlet.
Summary of the invention:
The objective of the invention is to overcome existing tube furnace technology is difficult to cracking heavy hydrocarbon, the utilization of regenerative furnace process heat and production efficiency is low, the sand furnaceman plants serious and many technological deficiencies of antiquated sand discharging of equipment attrition, in order to effectively utilize the petroleum resources of China, produce the most basic organic chemical industry's basic material, thereby provide a kind of heavy hydrocarbon cracking cleaning to produce the method and the pyrolysis gasification furnace system of low-carbon alkenes such as ethene.
The object of the present invention is achieved like this:
Pyrolysis gasification furnace system provided by the invention comprises that metallurgy high furnace 1 is main body, and its bottom is a cupola well 16, and the pneumatic outlet 14 of blast furnace 1 is communicated with waste heat boiler 3 by pipeline 15; It is characterized in that: described blast furnace 1 body of heater is divided into three sections, and wherein hypomere is combustion zone 8, and this combustion zone 8 is between body of heater 1/5～2/5 and the cupola well 16, and 1/5～3/5 highly is gasification cracking district 9 on it, and gasification cracking district 9 is that district 10 is finished in gasification with top; On the furnace body wall of combustion zone 8 and gasification cracking zone 9, have first gas inlet 12 and second gas inlet 13, finish on district's furnace body wall of 10 in gasification and to have a pneumatic outlet 14, on first gas inlet 12, be communicated with water vapor and oxygen channel, be communicated with heavy hydrocarbon and water vapor pipeline on second gas inlet 13.
The pneumatic outlet that also comprises waste heat boiler 3 is communicated with by the pipeline order with a clean unit 4, compressed element 5, ice chest unit 6 and separating unit 7.
The output channel that also is included in ice chest unit 6 is communicated with second gas inlet 13, and another pneumatic outlet of waste heat boiler 3 also is communicated with first gas inlet 12.
The output channel that also comprises separating unit 7 is communicated with the cold flow inlet of ice chest unit 6.
Wherein clean unit 4 can be a desulfurizing dust-collector; Wherein compressed element 5 can be a gas compressor; Wherein separating unit 7 can be gas-liquid separator.
Described metallurgy high furnace comprises: the retired steel-making of iron and steel enterprise, iron-smelting blast furnace or other blast furnace.
The method of low-carbon alkene is produced in heavy hydrocarbon cracking provided by the invention, may further comprise the steps:
1. at first in pyrolysis gasification stove of the present invention, fill coke or semicoke bed, the bottom of this filling bed is combustion zone 8, account for 1/5～2/5 of whole bed, for the heavy hydrocarbon pyrolysis provides needed heat, the middle part of this filling bed is gasification cracking district 9, account for 1/5～3/5 of whole bed, district 10 is finished for gasification in top, accounts for 1/5～3/5 of whole bed;
2. igniting blow-on;
3. the igniting back is to the coke bed aerating oxygen and the water vapor of combustion zone 8, and flow velocity is 0.9～15m
3/ s, the volume ratio of water vapor and oxygen is 3～7: 1, and coke bed is burnt to red-hot state; The oxygen that feeds is used for the burning of coke, and to provide scission reaction needed heat, the water vapor of feeding makes it temperature and remains between 1573～2073K (1300～1800 ℃) in order to control coke burned flame temperature;
4. when temperature remains between 1573～2073K (1300～1800 ℃), spray into heavy hydrocarbon and the water vapor that also atomizes through preheating by the coke bed of second gas inlet to gasification cracking district 9, perhaps in stove, add the solid cracking stock, this raw material can add after fragmentation, described heavy hydrocarbon and the process water steam weight ratio that sprays into through preheating and atomizing is 1: 0.75～10, and addition is that the inlet amount of heavy hydrocarbon is 0.2～50kg/s in the unit time; The coke in the coke products of combustion of combustion zone and water vapor and gasification cracking district reacts, the part of coke generation synthetic gas that gasified; Heavy hydrocarbon in the process that feeds the pyrolysis gasification stove by intense heating, to the coke surface cracking; The water vapor that feeds is in as the coke gasification raw material, as the thinner of hydrocarbon cracking reaction;
5. cracking and gasification product enter gasification and finish district 10, are 1～350m with take-off rate
3/ s, or 0.5～200kg/s derivation pyrolysis gasification stove make that the residence time of heavy hydrocarbon in the pyrolysis gasification stove is 0.01～0.5s, reclaim heats through waste heat boiler 3.
Also comprise step 6: reclaim heat through waste heat boiler 3 and deliver to clean unit 4; After the gas that purifies compressed again unit 5 compressions, with ice chest unit 6 and separating unit 7 separating and crackings and gasification product.
Described raw material can be used crude oil, heavy oil and residual oil, also can be polyolefine plastic waste etc.
Also comprise from the cracking of heavy hydrocarbon and gasification product and can isolate ethene, propylene, liquefied petroleum gas (LPG), synthetic gas (CO+H
2) etc., the liquid cracked oil that produces through condensation can be used as raw material and returns the pyrolysis gasification stove again, and further low-carbon alkene is produced in cracking, also can make processed oil behind the hydrogenation.
Also be included in the coking that cracking in the pyrolysis gasification stove produces and be deposited on coke surface, under the effect of bottom oxygen, be converted into heat, or react, produce synthetic gas, replenish the consumption of (or part is replenished) coke with water vapor with from the products of combustion of combustion zone.
Heavy hydrocarbon in the described step 4 is preheated to 323～623K (50～350 ℃), and water vapor is preheated to 623～923K (350～650 ℃).
The present invention is incorporated into the cracking and the heat supply of heavy hydrocarbon (crude oil, heavy oil, residual oil or polyolefine plastic waste etc.) in the same reactor, proportioning by control oxygen gas flow rate and oxygen and water vapor, the rate of oxidation of control coke and the method and apparatus of cracking temperature, its advantage is:
(1) thermo-efficiency height satisfies the interior processing requirement of heat supplies in a large number of hydrocarbon cracking short period of time;
(2) by regulating oxygen gas flow rate, the rate of oxidation of coke bed can be controlled,, the flame temperature of coke bed can be controlled by adjusting the ratio of oxygen and water vapor;
(3) the suitable heavy hydrocarbon of cooperation sprays into the derivation flow velocity of flow velocity and split product, can control the residence time of scission reaction, makes the processing requirement of short residence time(SRT) become possibility;
(4) high temperature in the pyrolyzer and higher gas flow rate cooperate a certain proportion of water vapor, make the processing requirement than low hydrocarbon partial pressure become possibility;
(5) coking that produces of cracking is deposited on coke surface, the intensive oxidizing reaction takes place under the effect of oxygen and be converted into heat, or gasify with water vapor and carbon dioxide reaction, has avoided the operation of frequent coke cleaning after the cracking apparatus coking; (the successive coking, burn and gasification,, improved the lysis efficiency of heavy hydrocarbon, reduced the frequency that adds the coke operation and the complicacy of cracking operation) for the cracking of successive heavy hydrocarbon provides heat condition;
(6) hearth structure of pyrolysis gasification furnace bottom makes the inorganic components in the heavy hydrocarbon at high temperature form slag with the flux Wingdale that adds, and discharges from the cinder notch of pyrolysis gasification stove, has avoided discharging the black burnt sand in a large number and the pollution that causes as the sand stove.
The present invention increases the entry and exit of raw material and product based on the retired blast furnace of iron and steel enterprise in the appropriate location of blast furnace, can transform the pyrolysis gasification stove as; With the coke of filling in the pyrolysis gasification stove as thermal source and thermal barrier, directly burning provides hydrocarbon cracking required heat, with heavy hydrocarbon (crude oil, heavy oil, residual oil or polyolefine plastic waste etc.) is cracking stock, with oxygen and water vapor is auxiliary agent, make heavy hydrocarbon that scission reaction take place in stove, produce low-carbon alkenes such as ethene, but while co-production synthesis gas (CO+H
2); The coking that scission reaction forms can replenish the consumption of (or part is replenished) coke.
The present invention relates to the cracking of heavy hydrocarbon (crude oil, heavy oil, residual oil or polyolefine plastic waste etc.), (1) except that cracking stock, coke, oxygen and water vapor also participate in reaction, and water vapor also has the effect of dilution split product simultaneously in the cracking technology process; (2) split product has low-carbon alkene, low-carbon alkanes, synthetic gas (CO+H
2) wait gaseous product, the condensable liquid product of cracked oil that is is also arranged, the solid product that also has the coking reaction to produce; (3) gaseous product (comprising the cracked oil under the temperature out) is derived pyrolyzer, reclaims heat after gas separation unit, separablely goes out ethene, propylene, liquefied petroleum gas (LPG), synthetic gas (CO+H
2) etc., the issuable liquid cracked oil of condensation can return pyrolyzer and make processed oil behind cracking or the hydrogenation once more, and the cracked coking is used for heat supply or produces synthetic gas; (4) this technology can seldom even not discharge pollutants except that discharging the slag solid waste, and is pollution-free substantially to environment.
Description of drawings
Fig. 1 is a pyrolysis gasification furnace system structural representation of the present invention
Fig. 2 is the comprehensive utilization process schematic flow sheet that utilizes the inventive method in pyrolyzer of the present invention
Fig. 3 is the process flow diagram of gasification cracking method of the present invention
The drawing explanation
1-blast furnace 2-coke inlet 3-waste heat boiler
4-clean unit 5-compressed element 6-ice chest unit
9-gasification cracking district, 7-separating unit 8-combustion zone
District 11-slag-drip opening 12-first gas inlet is finished in the 10-gasification
The 13-second gas inlet 14-pneumatic outlet 15-pipeline
The 16-cupola well
Embodiment
The present invention will be described in detail below in conjunction with drawings and Examples.
With reference to figure 1, present embodiment one metallurgy high furnace, particularly can adopt the retired blast furnace 1 of iron and steel enterprise to transform for main body, in its bottom is cupola well 16, described pyrolysis gasification furnace body is divided into three sections, being combustion zone 8 to body of heater 1/5 place on the cupola well 16, is gasification cracking district 9 below body of heater 1/5～3/5 height, and this gasification cracking district is that district 10 is finished in gasification with top; Have second gas inlet 13 on the furnace body wall that has first gas inlet 12 and gasification cracking zone 9 on 8 furnace body walls of combustion zone, finish on district's furnace body wall of 10 having a pneumatic outlet 14 in gasification, its pneumatic outlet 14 is communicated with waste heat boiler 3 by pipeline 15; Be communicated with water vapor and oxygen channel in first gas inlet 12, second gas inlet 13 is communicated with heavy hydrocarbon and water vapor pipeline.
With reference to figure 2
Present embodiment also be included in Fig. 1 iron and steel enterprise retired blast furnace 1 for main body and waste heat boiler 3 make pyrolyzer on increase again: clean unit 4, compressed element 5, ice chest unit 6 and separating unit 7; Wherein pneumatic outlet 14 is communicated with by the pipeline order with a desulfurizing dust-collector 4, gas compressor 5, ice chest 6 and gas-liquid separator 7; The output channel of ice chest 6 and gas-liquid separator 7 is communicated with second gas inlet 13, and the pneumatic outlet of waste heat boiler 3 is communicated with first gas inlet 12.Can also use other metallurgy high furnaces 1 to be main body in the present embodiment; The ice chest that ice chest unit 6 adopts Hangzhou system chlorine machine factory to produce.
The method that low-carbon alkene is produced in the heavy hydrocarbon cracking of present embodiment is to carry out in the gasification cracking stove of embodiment 1, and its concrete implementation step is as follows:
(1) in the pyrolysis gasification stove that embodiment 1 makes, fills coke or semicoke bed, the bottom of this filling bed is combustion zone 8, account for 1/5 of whole bed, for the heavy hydrocarbon pyrolysis provides needed heat, the middle part of this filling bed is gasification cracking district 9, account for 2/5 of whole bed, district 10 is finished for gasification in top, accounts for 2/5 of whole bed;
(2) igniting blow-on;
(3) to the coke bed aerating oxygen and the water vapor of combustion zone 8, flow velocity is 1.4m
3/ s, the volume ratio of water vapor and oxygen is 5: 1, and coke bed is burnt to red-hot state; The oxygen that feeds is used for the burning of coke, and to provide scission reaction needed heat, the water vapor of feeding makes it a little less than 2073K (1800 ℃) in order to control coke burned flame temperature;
(4) coke bed to gasification cracking district 9 sprays into heavy hydrocarbon and the water vapor that also atomizes through preheating, heavy hydrocarbon is preheated to 383K (110 ℃), water vapor is preheated to 723K (450 ℃), and heavy hydrocarbon and process steam weight ratio are 1: 1, and the inlet amount of heavy hydrocarbon is 0.278kg/s in the unit time; The coke in the coke products of combustion of combustion zone 8 and water vapor and gasification cracking district reacts, the part of coke generation synthetic gas that gasified; Heavy hydrocarbon in the process that feeds the pyrolysis gasification stove by intense heating, to the coke surface cracking; The water vapor that feeds is in as the coke gasification raw material, as the thinner of hydrocarbon cracking reaction;
(5) cracking and gasification product enter gasification and finish district 10, derive the pyrolysis gasification stove fast, and flow velocity is 2m
3/ s standard state volume after waste heat boiler 3 reclaims heat, is delivered to clean unit 4;
(6) after gas compressed unit 5 compressions, with ice chest unit 6 and separating unit 7 separating and crackings and gasification product.
What the present invention fed is pure oxygen, and the gasification of pyrolysis gasification stove is finished the composition of working off one's feeling vent one's spleen in the district and listed in table 1.
Under equal operational condition, form the result with the splitting gas of regenerative furnace pyrolysis Shandong crude oil gained and also be shown in table 1.
Table 1 Shandong crack crude gas data on bulk analysis (volume %)
| The exit gas composition | Exit gas is formed | |
| The present invention | Regenerative furnace [5] | |
| H 2 CO N 2 CH 4 CO 2 C 2H 4 C 2H 6 C 3H 6 C 3H 8 C 4H 8-1 C 4H 6(diene) | 21.89 46.09 -α 14.43 1.44 11.41 0.77 3.15 0.19 0.05 0.58 | 16.64 2.23 2.97 35.23 3.52 27.85 1.88 7.69 0.47 0.11 1.41 |
| Add up to | 100.00 | 100.00 |
The present invention adopts the total oxygen technology, replaces document 5: Danyang county fertilizer plant. and petrochemical complex .1975,4 (supplementary issues): the air among the 2-9. promotes the burning of coke.
Wherein the operational condition of regenerative furnace pyrolysis Shandong crude oil is the condition of document 5 records: crude oil is preheated to 383K (110 ℃), atomizing oil pressure 10kg/cm
2, crude oil is 1: 1 with process steam ratio, and steam temperature is 723K (450 ℃), and pressure is 4.5kg/cm
2, feeding air in certain amount, cracking temperature is 1073K (800 ℃).
In the pyrolysis gasification stove that embodiment 1 makes, process flow sheet by Fig. 2 comprehensive utilization carries out, the charging of this pyrolysis gasification stove comprises oxygen, water vapor and cracking stock, wherein the source of most of water vapor is from waste heat boiler 3 heat exchange, cracking stock is except heavy hydrocarbon, and low-carbon alkanes such as the methane that part is returned from ice chest unit 6 and separating unit 7, ethane are as raw material.
The temperature of the pneumatic outlet 14 of pyrolysis gasification stove is 1073～1173K (800～900 ℃), and cracking and gasification product feed waste heat boiler, and after heat recuperation, gas temperature is reduced to below the 573K (300 ℃).Meanwhile, being used for refrigerating water endothermic transition is water vapor, imports the pyrolysis gasification stove and participates in reaction.
The pyrolysis gasification product that comes out from waste heat boiler 3 is after desulfurizing dust-collector (clean unit 4) purifies, send into gas compressor 5, gaseous product after compression enters ice chest unit 6 with a certain amount of cold of importing and separates, and successively liquefaction separates according to the difference of each component boiling point.The cold that each liquid parts is entrained, the interchanger through ice chest discharges entrained most of cold once more, is used for from the refrigerated separation of the pyrolysis gasification product of gas compressor 5 inputs.
The gaseous fraction that obtains from the ice chest separation has synthetic gas (CO+H
2), low-carbon alkene, low-carbon alkanes etc., wherein synthetic gas (CO+H
2) separate as industrial chemicals with low-carbon alkene, alkane components such as low-carbon alkanes such as methane, ethane return behind the pyrolysis gasification stove as cracking stock cracking once more.
Material circulation and energy through this process utilize again, when further improving the yield of low-carbon alkene, the heat and the cold return course that make in the technological process to be produced are that process is used, meet the requirement of modernized chemical engineering process, can realize that matter and energy utilizes to greatest extent in the technological process.
According to this comprehensive utilization process, the operational condition gained of employing sand stove crack crude is worked off one's feeling vent one's spleen to form and be the results are shown in table 2.
The operational condition such as the document of the crack crude of sand stove: Shanxi Province's chemistry of fuel institute. petrochemical complex .1975,4 (1): 18-27. is described: the crude oil feeding amount is 1100kg/h, crude oil is 1: 1.15 with the water vapor ratio, and cracking temperature is 1013K (740C), and the residence time is 0.498s.Its composition result that works off one's feeling vent one's spleen also lists in table 2, to show contrast.
Table 2 crack crude exit gas product is formed result (volume %)
| The exit gas composition | Exit gas is formed | |
| The present invention | Sand stove [6] | |
| CO H 2 CH 4 C 2H 4 C 2H 6 C 3H 6 C 3H 8 C 4H 8-1 C 2H 2 CO 2Aromatics other | 45.23 18.49 9.54 14.38 2.03 5.88 0.12 0.02 0.03 0.12 0.54 3.62 | - 8.6 24.04 36.22 5.12 14.8 0.3 0.05 0.081 0.3 1.353 9.136 |
| Amount to | 100.00 | 100.00 |
Claims (8)
1. a pyrolysis gasification furnace system comprises that metallurgy high furnace (1) is main body, and its bottom is cupola well (16), and the pneumatic outlet (14) of blast furnace (1) is communicated with waste heat boiler (3) by pipeline (15); It is characterized in that: described blast furnace (1) 1 body of heater is divided into three sections, wherein hypomere is combustion zone (8), this combustion zone (8) is between body of heater 1/5～2/5 and the cupola well (16), and 1/5～3/5 highly is gasification cracking district (9) on it, and gasification cracking district (9) are that district (10) is finished in gasification with top; On the furnace body wall of combustion zone (8) and gasification cracking zone (9), have first gas inlet (12) and second gas inlet (13), finish in gasification on the furnace body wall of district (10) and have a pneumatic outlet (14), go up connection water vapor and oxygen channel in first gas inlet (12), second gas inlet (13) are gone up and are communicated with heavy hydrocarbon and water vapor pipeline.
2. by the described pyrolysis gasification furnace system of claim 1, it is characterized in that: comprise that also the pneumatic outlet of waste heat boiler (3) is communicated with by the pipeline order with a clean unit (4), compressed element (5), ice chest unit (6) and separating unit (7).
3. by the described pyrolysis gasification furnace system of claim 1, it is characterized in that: the output channel that also is included in ice chest unit (6) and separating unit (7) is communicated with second gas inlet (13), and another pneumatic outlet of waste heat boiler (3) is communicated with first gas inlet (12).
4. by claim 1,2 or 3 described each pyrolysis gasification furnace systems, it is characterized in that: described clean unit (4) is a desulfurizing dust-collector; Described compressed element (5) is a gas compressor; Described separating unit (7) is a gas-liquid separator.
5. an application rights requires 1 described pyrolysis gasification stove cracking to produce the method for low-carbon alkene, it is characterized in that: comprise that order is carried out as follows:
(1) fill coke or semicoke bed in pyrolysis gasification stove of the present invention, the bottom of this filling bed is the combustion zone, accounts for 1/5～2/5 of whole bed, the middle part of this filling bed is the gasification cracking district, account for 1/5～3/5 of whole bed, the district is finished for gasification in top, accounts for 1/5～3/5 of whole bed;
(2) igniting blow-on; Coke bed aerating oxygen and water vapor to the combustion zone, the volume ratio of its water vapor and oxygen are 3～7: 1; Flow velocity is 0.9～15m
3/ s burns coke bed to red-hot state; Making it temperature remains between 1300～1800 ℃;
(3) when temperature remains between 1300～1800 ℃, spray into heavy hydrocarbon and the water vapor that also atomizes through preheating by the coke bed of second gas inlet to gasification cracking district (9), perhaps in stove, add the solid cracking stock, described heavy hydrocarbon and the process water steam weight ratio that sprays into through preheating and atomizing is 1: 0.75～10, and addition is that the inlet amount of heavy hydrocarbon is 0.2～50kg/s in the unit time;
(4) cracking and gasification product enter gasification and finish the district, are 1～350m with take-off rate
3/ s, or 0.5～200kg/s derivation pyrolysis gasification stove make that the residence time of heavy hydrocarbon in the pyrolysis gasification stove is 0.01～0.5s, reclaim heat through waste heat boiler.
6. produce the method for low-carbon alkene by the cracking of the described pyrolysis gasification stove of claim 5, it is characterized in that: the heavy hydrocarbon in the described step (4) is preheated to 50～350 ℃, and water vapor is preheated to 350～650 ℃.
7. produce the method for low-carbon alkene by the cracking of the described pyrolysis gasification stove of claim 5, it is characterized in that: comprise the steps: that also reclaiming heat through waste heat boiler (3) delivers to clean unit (4); After the compressed again unit of gas (5) compression that purifies, with ice chest unit (6) and separating unit (7) separating and cracking and gasification product.
8. produce the method for low-carbon alkene by the cracking of the described pyrolysis gasification stove of claim 5, it is characterized in that: described raw material comprises crude oil, heavy oil and residual oil; Or polyolefine plastic waste; Or also comprise from the cracking of heavy hydrocarbon and gasification product and isolate ethene, propylene, liquefied petroleum gas (LPG), synthetic gas CO+H
2After the liquid cracked oil that condensation produces.
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| CN112538371B (en) * | 2019-09-23 | 2022-02-25 | 中国石油大学(北京) | Heavy oil lightening coupling reaction device |
| US11319262B2 (en) | 2019-10-31 | 2022-05-03 | Eastman Chemical Company | Processes and systems for making recycle content hydrocarbons |
| US11945998B2 (en) | 2019-10-31 | 2024-04-02 | Eastman Chemical Company | Processes and systems for making recycle content hydrocarbons |
| WO2021087054A1 (en) * | 2019-10-31 | 2021-05-06 | Eastman Chemical Company | Pyrolysis method and system for recycled waste |
| WO2021092306A1 (en) | 2019-11-07 | 2021-05-14 | Eastman Chemical Company | Recycle content alpha olefins and fatty alcohols |
| WO2021092305A1 (en) | 2019-11-07 | 2021-05-14 | Eastman Chemical Company | Recycle content mixed esters and solvents |
-
2003
- 2003-10-17 CN CN 200310100482 patent/CN1259391C/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101451702B (en) * | 2007-11-30 | 2011-04-20 | 上海吴泾化工有限公司 | Cracking gas heat comprehensive utilization method and exhaust heat boiler using the method |
| WO2012034295A1 (en) * | 2010-09-17 | 2012-03-22 | 林月蓉 | Apparatus and method for preparing lower olefin by cracking reaction |
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| CN1609169A (en) | 2005-04-27 |
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