CN202936381U - Heavy oil pyrolysis and gasification device with coupled combined type lifting pipe and downer reactor - Google Patents
Heavy oil pyrolysis and gasification device with coupled combined type lifting pipe and downer reactor Download PDFInfo
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- CN202936381U CN202936381U CN 201220610248 CN201220610248U CN202936381U CN 202936381 U CN202936381 U CN 202936381U CN 201220610248 CN201220610248 CN 201220610248 CN 201220610248 U CN201220610248 U CN 201220610248U CN 202936381 U CN202936381 U CN 202936381U
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Abstract
The utility model provides a heavy oil pyrolysis and gasification device with coupled combined type lifting pipe and downer reactor. The heavy oil pyrolysis and gasification device is characterized in that a downer reaction pipe is communicated with a combined type lifting pipe gasification reactor through a refeeder, a stripper and a flow regulator to form a circular reaction system; symmetrical efficient atomizing nozzles are arranged at the upper part of the downer reaction pipe, a gas-solid quick disconnector is mounted at the lower part of the downer reaction pipe, the gas outlet of the gas-solid quick disconnector is a pyrolysis gas outlet, the solid outlet of the gas-solid quick disconnector is led into the stripper, and the outlet of the stripper is communicated with the lower part of the combined type lifting pipe gasification reactor through the flow regulator; a steam inlet and an oxidant inlet are formed at the lower part of the combined type lifting pipe gasification reactor, and a synthesis gas separator is arranged at the upper part; and the solid out of the synthesis gas separator is obliquely led into the refeeder, the outlet of the refeeder is connected with the top of the downer reaction pipe, and the gas outlet of the synthesis gas separator is connected with a synthesis gas outlet through a heat exchanger.
Description
1. technical field
The utility model provides Heavy Oil Thermal and the gasification installation of Combined type lifting riser and descending reactor coupling, belongs to the refining of petroleum field.
2. background technology
The heavy oil lighting is one of important topic of world refining of petroleum.In the most of crude oil of China, residual oil content is high, and lightweight oil content is low, and the introduction of the continuous growth of some mink cell focuses (viscous crude) output in recent years and the external heavy crude of part makes heavy oil lighting problem more outstanding in addition.The heavy oil upgrading method often has the methods such as catalytic cracking, solvent deasphalting, visbreaking, coking, thermally splitting, heavy-oil hydrogenation, generally speaking, nothing more than hydrogenation and the large class of decarburization two, wherein heavy oil decarburization processing is the major way of current refining of petroleum, and the reasonable utilization of deviating from carbon does not obtain fine solution always.Mainly contain heavy oil catalytic pyrolysis, flexicoking, fluid coking, heavy oil fluidized upgrading etc. in heavy oil solid phase carrier circulation cracking technology.Heavy oil catalytic pyrolysis is except the purpose product that obtains (petrol and diesel oil and alkene industrial chemicals), the carbon residue that the removes heat release of burning in revivifier, part heatable catalyst is as the thermal source of cracking, a part produces steam with the heat collector heat-obtaining and sends outside or generate electricity, temperature of reaction is low approximately 500 ℃-650 ℃, higher to the heavy oil ingredient requirement, do not reach fully effectively utilizing petroleum resources; Flexicoking and fluid coking temperature of reaction are low approximately 450 ℃-600 ℃, it is mainly the wax tailings of producing coker gasoline, diesel oil and being used as fcc raw material, char combustion partly circulates and produces synthetic gas as thermal barrier, partial gasification, but pyrolysis time is long, and yield of light oil is lower; Heavy oil fluidized upgrading (as the HCC technique of the ART technique of Engelhardt moral exploitation, Luoyang Petrochemical designing institute etc.) adopts the circulating fluidized bed technique similar to heavy oil catalytic cracking process, approximately 400 ℃-600 ℃ of temperature of reaction, pyrolysis time is short, yield of light oil is higher, but the carbon residue that removes is not utilized effectively always.
In addition because national requirements for environmental protection is more and more higher, refining of petroleum enterprise needs again a large amount of hydrogen to carry out hydrofining to light-end products to satisfy qualified vehicle fuel with production, but each Petrochemical Enterprises lacks a large amount of cheap sources of hydrogen at present.
How to develop most economical, the technology and equipment of cleaning, the most reasonable and good heavy oil of maximum using, realize without scorification, will become the China's oil worker and compel key subjects to be solved.
3. summary of the invention
the purpose of this utility model is exactly Heavy Oil Thermal and the gasification installation of a kind of Combined type lifting riser and the coupling of descending reactor for the deficiency that overcomes existing heavy oil upgrading device existence, form circulating system by descending reaction tubes and the coupling of Combined type lifting riser gasifying reactor, descending reaction tubes pyrolysis heavy oil is produced lightweight oil or alkene, the synthetic gas hydrogen making is produced in the gasification of Combined type lifting riser gasifying reactor, utilize the steam gasification heat absorption to solve the superfluous difficult problem of heat of burnt regeneration, utilize the Combined type lifting riser to strengthen gasification reaction, elimination riser tube bottom is difficult to ignition, reduce height for reactor, can produce lightweight oil or alkene, can obtain again a large amount of cheap hydrogen resources, realize that the low reserve of heavy oil upgrading is efficiently without scorification.
The technical solution of the utility model:
Heavy Oil Thermal and the gasification installation of Combined type lifting riser and the coupling of descending reactor are comprised of synthetic gas separator, material returning device, high-efficiency atomizing nozzle, descending reaction tubes, gas-solid quick disconnector, pyrolysis gas outlet, stripper, flow regulator, steam-in, oxidant inlet, Combined type lifting riser gasifying reactor, interchanger, syngas outlet.Descending reaction tubes is communicated with Combined type lifting riser gasifying reactor by material returning device, stripper and flow regulator and forms a circulating reaction system; Descending reaction tubes top is provided with symmetrical high-efficiency atomizing nozzle, the gas-solid quick disconnector is equipped with in the bottom, gas-solid quick disconnector pneumatic outlet is pyrolysis gas outlet, gas-solid quick disconnector solid outlet passes into stripper, and stripper outlet is communicated with Combined type lifting riser gasifying reactor bottom by flow regulator; Combined type lifting riser gasifying reactor bottom is provided with steam-in and oxidant inlet, and top is provided with the synthetic gas separator; Synthetic gas separator solid outlet passes into material returning device under tiltedly, and the material returning device outlet connects descending reaction tubes top, and the outlet of synthetic gas separator gas is connected with syngas outlet by interchanger.
The mid point of descending reaction tubes and Combined type lifting riser gasifying reactor is in same level, and the ratio of its equivalent diameter is 1:1 ~ 2.5, and Combined type lifting riser gasifying reactor length is 10-25m, and descending reaction tubes is than the short 3-12m of Combined type lifting riser gasifying reactor.
Combined type lifting riser gasifying reactor is comprised of the turbulent fluidized bed of bottom and the reactor that carries on top, the turbulent fluidized bed diameter is 2-4 times of riser tube gasifying reactor equivalent diameter, carrying reactor is to be formed by connecting by the concentric reducer pipe fitting by the big or small straight tube that diameter is riser tube gasifying reactor equivalent diameter different multiples, and the diameter ratio of big or small straight tube is 1.2 ~ 2:1.
Material returning device is a kind of in the on-mechanical valves such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device.
Gas-solid quick disconnector and synthetic gas separator are a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator.
Flow regulator is a kind of in the on-mechanical valves such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device and the mechanical valve such as hydraulic pressure slip plug valve, electronic slip plug valve.
The present invention is described in detail characteristics of the present invention with embodiment.
4. description of drawings
Accompanying drawing is structural representation of the present utility model.
The drawing of accompanying drawing is described as follows:
1. synthetic gas separator, 2. material returning device, 3. high-efficiency atomizing nozzle, 4. descending reaction tubes, 5. gas-solid quick disconnector, 6. pyrolysis gas outlet, 7. flow regulator, 8. steam-in, 9. oxidant inlet, 10. Combined type lifting riser gasifying reactor, 11. interchanger, 12. syngas outlet, 13. strippers.
Below in conjunction with drawings and Examples in detail process characteristic of the present utility model is described in detail.
5. embodiment
embodiment, Heavy Oil Thermal and the gasification installation of Combined type lifting riser and the coupling of descending reactor, by synthetic gas separator (1), material returning device (2), high-efficiency atomizing nozzle (3), descending reaction tubes (4), gas-solid quick disconnector (5), pyrolysis gas outlet (6), stripper (13), flow regulator (7), steam-in (8), oxidant inlet (9), Combined type lifting riser gasifying reactor (10), interchanger (11), syngas outlet (12) forms, descending reaction tubes (4) is by material returning device (2), stripper (13) and flow regulator (7) are communicated with Combined type lifting riser gasifying reactor (10) and form a circulating reaction system, descending reaction tubes (4) top is provided with symmetrical high-efficiency atomizing nozzle (3), gas-solid quick disconnector (5) is equipped with in the bottom, gas-solid quick disconnector (5) pneumatic outlet is pyrolysis gas outlet (6), gas-solid quick disconnector (5) solid outlet passes into stripper (13), and stripper (13) outlet is communicated with Combined type lifting riser gasifying reactor (10) bottom by flow regulator (7), Combined type lifting riser gasifying reactor (10) bottom is provided with steam-in (8) and oxidant inlet (9), top is provided with synthetic gas separator (1), pass into material returning device (2) under synthetic gas separator (1) solid outlet is oblique, material returning device (2) outlet connection descending reaction tubes (4) top, synthetic gas separator (1) pneumatic outlet is connected with syngas outlet (12) by interchanger (11).
The mid point of descending reaction tubes (4) and Combined type lifting riser gasifying reactor (10) is in same level, its diameter ratio is 1:1 ~ 2.5, Combined type lifting riser gasifying reactor (10) length is 10-25m, and descending reaction tubes (4) is than the short 3-12m of Combined type lifting riser gasifying reactor (10).
Combined type lifting riser gasifying reactor (10) is comprised of the turbulent fluidized bed of bottom and the reactor that carries on top, the turbulent fluidized bed diameter is 2-4 times of riser tube gasifying reactor (10) equivalent diameter, carrying reactor is to be formed by connecting by the concentric reducer pipe fitting by the big or small straight tube that diameter is riser tube gasifying reactor (10) equivalent diameter different multiples, and the diameter ratio of big or small straight tube is 1.2 ~ 2:1.
Material returning device (2) is a kind of in the on-mechanical valves such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device.
Gas-solid quick disconnector (5) and synthetic gas separator (1) are a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator.
Flow regulator (7) is a kind of in the mechanical valve such as the on-mechanical valves such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device and hydraulic pressure slip plug valve, electronic slip plug valve.
During concrete operation, high-efficiency atomizing nozzle (3) will be preheating to the heavy oil of 180 ℃-350 ℃ and spray into descending reaction tubes (4) top from descending reaction tubes (4) opening for feed, mist of oil mixes with 800 ℃ that flow down from material returning device (2)-1100 ℃ of high-temp solid carriers, heating, vaporization and pyrolysis; After oil gas and coking, the downward high speed following current of solid carrier is carried out gas solid separation to the gas-solid quick disconnector (5) bottom descending reaction tubes (4); Oil gas advances separation column from pyrolysis gas outlet (6) to be separated, and slurry oil returns to heavy oil and recycles, and other are as output of products; Enter Combined type lifting riser gasifying reactor (10) bottom and the oxygen and the steam generation gasification reaction that enter from vapour inlet (8) and oxidant inlet (9) by flow director (7) after the solid carrier stripping after coking, after 850 ℃-1200 ℃ of temperature of reaction, the synthetic gas separator (1) that the synthetic gas of generation and high-temp solid carrier upwards at a high speed flow to Combined type lifting riser gasifying reactor (10) top carries out gas solid separation; The high-temp solid carrier that separates flows into material returning device (2) to be continued to recycle as the Heavy Oil Thermal thermal source, synthetic gas through interchanger (11) heat exchange after from syngas outlet (12) as output of products, realize that heavy oil processes without scorification.
Oxygenant can be selected in oxygen, oxygen-rich air and air a kind of.
Heavy Oil Thermal and the gasification installation of Combined type lifting riser provided by the utility model and the coupling of descending reactor, form circulating system by descending reaction tubes and the coupling of Combined type lifting riser gasifying reactor, descending reaction tubes pyrolysis heavy oil is produced lightweight oil or alkene, the synthetic gas hydrogen making is produced in the gasification of Combined type lifting riser gasifying reactor, utilize the steam gasification heat absorption to solve the superfluous difficult problem of heat of burnt regeneration, utilize the Combined type lifting riser to strengthen gasification reaction, elimination riser tube bottom is difficult to ignition, reduction height for reactor 50% left and right, facility investment reduces more than 20%, can improve lightweight oil or olefin yields 5%-30%, can obtain again a large amount of cheap hydrogen resources (cost is about 50%), realize that the low reserve of heavy oil upgrading is efficiently without scorification.
Claims (6)
- Combined type lifting riser and descending reactor the coupling Heavy Oil Thermal and gasification installation, formed by synthetic gas separator, material returning device, high-efficiency atomizing nozzle, descending reaction tubes, gas-solid quick disconnector, pyrolysis gas outlet, stripper, flow regulator, steam-in, oxidant inlet, Combined type lifting riser gasifying reactor, interchanger, syngas outlet, it is characterized in that descending reaction tubes is communicated with circulating reaction system of composition by material returning device, stripper and flow regulator with Combined type lifting riser gasifying reactor; Descending reaction tubes top is provided with symmetrical high-efficiency atomizing nozzle, the gas-solid quick disconnector is equipped with in the bottom, gas-solid quick disconnector pneumatic outlet is pyrolysis gas outlet, gas-solid quick disconnector solid outlet passes into stripper, and stripper outlet is communicated with Combined type lifting riser gasifying reactor bottom by flow regulator; Combined type lifting riser gasifying reactor bottom is provided with steam-in and oxidant inlet, and top is provided with the synthetic gas separator; Synthetic gas separator solid outlet passes into material returning device under tiltedly, and the material returning device outlet connects descending reaction tubes top, and the outlet of synthetic gas separator gas is connected with syngas outlet by interchanger.
- 2. carry according to claim 1 Heavy Oil Thermal and the gasification installation of the coupling of the Combined type lifting riser stated and descending reactor, it is characterized in that the mid point of descending reaction tubes and Combined type lifting riser gasifying reactor is in same level, the ratio of its equivalent diameter is 1:1 ~ 2.5, Combined type lifting riser gasifying reactor length is 10-25m, and descending reaction tubes is than the short 3-12m of Combined type lifting riser gasifying reactor.
- 3. carry according to claim 2 the Combined type lifting riser gasifying reactor of stating, it is characterized in that Combined type lifting riser gasifying reactor is comprised of the turbulent fluidized bed of bottom and the reactor that carries on top, the turbulent fluidized bed diameter is 2-4 times of riser tube gasifying reactor equivalent diameter, carrying reactor is to be formed by connecting by the concentric reducer pipe fitting by the big or small straight tube that diameter is riser tube gasifying reactor equivalent diameter different multiples, and the diameter ratio of big or small straight tube is 1.2 ~ 2:1.
- 4. carry according to claim 1 Heavy Oil Thermal and the gasification installation of the coupling of the Combined type lifting riser stated and descending reactor, it is characterized in that material returning device is a kind of in the on-mechanical valves such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device.
- 5. carry according to claim 1 Heavy Oil Thermal and the gasification installation of the coupling of the Combined type lifting riser stated and descending reactor, it is characterized in that gas-solid quick disconnector and synthetic gas separator are a kind of in vertical cyclone separator, horizontal cyclone separator, inertial separator.
- 6. carry according to claim 1 Heavy Oil Thermal and the gasification installation of the coupling of the Combined type lifting riser stated and descending reactor, it is characterized in that flow regulator is a kind of in the on-mechanical valve such as L-type material returning device, U-shaped material returning device, J type material returning device and N-type material returning device and the mechanical valve such as hydraulic pressure slip plug valve, electronic slip plug valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220610248 CN202936381U (en) | 2012-11-16 | 2012-11-16 | Heavy oil pyrolysis and gasification device with coupled combined type lifting pipe and downer reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220610248 CN202936381U (en) | 2012-11-16 | 2012-11-16 | Heavy oil pyrolysis and gasification device with coupled combined type lifting pipe and downer reactor |
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|---|---|
| CN202936381U true CN202936381U (en) | 2013-05-15 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220610248 Expired - Fee Related CN202936381U (en) | 2012-11-16 | 2012-11-16 | Heavy oil pyrolysis and gasification device with coupled combined type lifting pipe and downer reactor |
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| CN (1) | CN202936381U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102965139A (en) * | 2012-11-16 | 2013-03-13 | 中国石油大学(华东) | Heavy oil pyrolysis and gasification device coupling combined type lifting pipe and downstream reactor |
| CN109652104A (en) * | 2017-10-12 | 2019-04-19 | 中国石油化工股份有限公司 | Down-flow fluidized bed using ECT-air flow bed is pyrolyzed-gasifies integral method and device |
-
2012
- 2012-11-16 CN CN 201220610248 patent/CN202936381U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102965139A (en) * | 2012-11-16 | 2013-03-13 | 中国石油大学(华东) | Heavy oil pyrolysis and gasification device coupling combined type lifting pipe and downstream reactor |
| CN109652104A (en) * | 2017-10-12 | 2019-04-19 | 中国石油化工股份有限公司 | Down-flow fluidized bed using ECT-air flow bed is pyrolyzed-gasifies integral method and device |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130515 Termination date: 20131116 |