CN212687968U - Coal hydrogenation residue coking system - Google Patents
Coal hydrogenation residue coking system Download PDFInfo
- Publication number
- CN212687968U CN212687968U CN202021555249.6U CN202021555249U CN212687968U CN 212687968 U CN212687968 U CN 212687968U CN 202021555249 U CN202021555249 U CN 202021555249U CN 212687968 U CN212687968 U CN 212687968U
- Authority
- CN
- China
- Prior art keywords
- coking
- area
- reduced pressure
- export
- hydrogenation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a coal hydrogenation residue coking system, including feedstock line, the hydrogenation ware, hot high pressure separator, feedstock line is connected to the hydrogenation ware import, the hot high pressure separator of hydrogenation ware exit linkage is imported, hot high pressure separator top sets up the gas phase export, the bottom is the thick liquids export, the thick liquids export of hot high pressure separator bottom is connected to the feed inlet that the formula evaporation coking device was extruded to the screw rod through the solvent pump, this formula evaporation coking device is extruded to the screw rod sets up reduced pressure distillation district and coking area, the reduced pressure distillation district is provided with the export of oil phase evaporation product, oil phase evaporation product export is through evaporation product pipe connection to knockout drum, the coking area is provided with distillate oil gas phase export and coke export. The utility model discloses a coal hydrogenation residue coking system, coal hydrogenation residue carry out the vacuum distillation in double screw extruder, and the wax oil is drawed out, and remaining thick liquids then continue to coke in double screw extruder, and condensation reaction generates partial light distillate oil and retrieves.
Description
Technical Field
The utility model belongs to the technical field of coal hydrogenation processing system, especially, coal hydrogenation residue coking system.
Background
As is well known, the coal hydrogenation theory is that coal is subjected to hydrogenation reaction with hydrogen at 350-. The product at room temperature is composed mainly of solid residues and highly viscous liquid residues together with gas/liquid phase hydrocarbons. The catalytic hydrogenation process of coal has wide application range aiming at raw materials, almost all coal can be processed by the process, anthracite is preferred, and the ash content is low.
The residue of coal hydrogenation is difficult to treat, and at present, the residue is mainly treated by transportation after solidification and granulation. The treatment mode mainly comprises incineration and landfill, the incineration additional value is very low, and the landfill has great damage to the environment. And if the wax oil content in the residue is high, the softening point of the residue is low, granulation cannot be realized, and the plant is frequently shut down.
The existing coal hydrogenation processes, including boiling bed and suspension bed processes, have a common characteristic that coal hydrogenation residues are required to be separated from gas-phase and liquid-phase products in a hot high-pressure separation tank. The operation conditions of the hot high-pressure separation tank are the same as the reaction temperature and the reaction pressure of the coal hydrogenation reaction. The separated coal hydrogenation residue comprises valuable wax oil, solid material (mainly composed of unconverted coal, ash and catalyst), liquid fraction with low volatility and intermediate product with high viscosity (mainly composed of asphaltene and colloid). The further processing and recovery of the coal hydrogenation residue is valuable, mainly the wax oil is separated from the coal hydrogenation residue for recovery, part of the coking gasoline and diesel oil and the like are recovered, and the coke can be directly sold as a product.
Coking, vacuum distillation, etc. may be applied to the processing of coal hydrogenation residues, so that the wax oil in the residue is extracted. The recovered wax oil can be returned as a feed to the coal hydrogenation reaction. Conventional coking requires that the coal hydrogenation residue be conducted as a feed in a coke oven. However, in this process, the light wax oil is substantially converted to coke, which is wasted. And the separation of wax oil in the coal hydrogenation residue can be realized by vacuum distillation, and the recovered wax oil can be used as circulating solvent oil to be used as a feed to be mixed with coal powder. These oil components can also be further hydrogenated under relatively mild conditions to produce gasoline and diesel. However, the conventional process has a critical problem in that it is very difficult to remove the residue from the vacuum distillation column and transfer the residue to a downstream apparatus for further processing due to the high solid content and high viscosity of the residue after vacuum distillation.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome prior art's is not enough, provides a coal hydrogenation residue coking system, and coal hydrogenation residue carries out the vacuum distillation in double screw extruder, and the wax oil is drawed out, and remaining thick liquids then continues to coke in double screw extruder, and condensation reaction generates partial light distillate oil and retrieves.
The utility model provides a its technical problem realize through following technical scheme:
the utility model provides a coal hydrogenation residue coking system, includes feedstock line, hydrogenation ware, hot high pressure separator, and feedstock line is connected to the hydrogenation ware import, and the hydrogenation ware exit linkage hot high pressure separator import, hot high pressure separator top set up the gas phase export, and the bottom is the thick liquids export, its characterized in that: the slurry outlet at the bottom of the thermal high-pressure separator is connected to a feed inlet of a screw extrusion type evaporation coking device through a solvent pump, the screw extrusion type evaporation coking device is provided with a reduced pressure distillation area and a coking area, the reduced pressure distillation area is provided with an oil phase evaporation product outlet, the oil phase evaporation product outlet is connected to a separation tank through an evaporation product pipeline, and the coking area is provided with a distillate oil gas phase outlet and a coke outlet.
And the separating tank connected with the reduced pressure distillation area is connected with a vacuum pump, and the reduced pressure distillation area is at negative pressure and the pressure is 0.01-0.5 bara.
And a separation zone is arranged between the reduced pressure distillation zone and the coking zone, and a material port is formed in the separation zone.
Moreover, the screw extrusion type evaporation coking device adopts a double-screw extruder.
Moreover, a feed inlet of the screw extrusion type evaporation coking device is arranged on the bottom surface of the shell of the screw extrusion type evaporation coking device; the reduced pressure distillation area is provided with an oil phase evaporation product outlet which is arranged at the upper part of the shell of the screw extrusion type evaporation coking device.
The utility model discloses an advantage and beneficial effect do:
1. the coal hydrogenation residue coking system of the utility model, the coal hydrogenation residue is decompressed and distilled in the screw extrusion type evaporation coking device, in the process, the wax oil is extracted, the residual slurry is continuously coked in the extruder, and in the coking process, the condensation reaction can generate partial light distillate oil and recover the light distillate oil; during the process of carrying out reduced pressure distillation and coking on the coal hydrogenation residue, materials can continuously move forward in the extruder by a screw in the extruder, the extruder conveys slurry to pass through a reduced pressure distillation area and a coking area of the device, the viscosity of the residual materials is continuously increased along with continuous gasification of a liquid phase, in the process, firstly, volatile components (mainly wax oil components) are extracted from the slurry in the reduced pressure distillation area, and then the residue passes through the coking area, wherein the volatile components are subjected to thermal cracking reaction to generate coking distillate oil, and the distillate oil is also extracted.
2. The coal hydrogenation residue coking system of the utility model, the double screw extruder can be operated under the negative pressure environment, and has the function of gas or steam extraction, since the coal hydrogenation process reaches the industrialized scale, the difficulty of oil-solid separation of the hydrogenation residue has existed for a long time, in the reduced pressure distillation zone of the double screw extruder, the recommended pressure is 0.01-0.5bara (optimum value: 0.05-0.1bara), in the reduced pressure distillation zone of the screw extruder, from the slurry inlet to the outlet of the zone, the pressure keeps constant negative pressure, the temperature keeps constant, which is 250-, the remaining slurry, which is essentially composed of a liquid phase of asphaltenes/gums and solids such as ash and catalyst in the coal, continues onwards to the coking zone.
3. The utility model discloses a coal hydrogenation residue coking system, be provided with the subregion between vacuum distillation district and the coking district, this subregion system has the material mouth, carry out the suitable partition of vacuum zone and atmospheric region to vacuum distillation district and coking district, but need guarantee the transmission of material, coking district operating pressure is the ordinary pressure, the temperature is 400 + and makes good for 600 ℃, the constant temperature operation, in the coking process, along with dwell time's increase, liquid phase heavy oil can carry out the thermal cracking condensation reaction, generate coke and light distillate oil, the back of distillate oil gasification, but the cooling is retrieved, the distillate oil that draws out in the coking district of screw extruder also can be used as solvent naphtha feeding and buggy mixture, circulation coal hydrogenation front end. Or further hydrogenation treatment to produce gasoline and diesel oil.
4. In the coal hydrogenation residue coking system, the feed inlet of the screw extrusion type evaporation coking device is arranged at the bottom surface of the shell of the screw extrusion type evaporation coking device, and the feeding under the bottom liquid level can realize the sealing of the inlet of the pipeline; the reduced pressure distillation area is provided with an oil phase evaporation product outlet which is arranged at the upper part of the shell of the screw extrusion type evaporation coking device, so that the material is convenient to discharge.
5. The utility model discloses a coal hydrogenation residue coking system is applicable to the processing of taking place all hydrogenation residues at high-pressure coal hydrogenation technology, and coal hydrogenation residue carries out the vacuum distillation in double screw extruder, and the wax oil is drawed out, and remaining thick liquids then continue to coke in double screw extruder, and condensation reaction generates partial light distillate oil and retrieves.
Drawings
Fig. 1 is a flow chart of the system of the present invention.
Reference numerals:
1-a hydrogenation reactor, 2-a hot high-pressure separator, 3-a solvent pump, a 4-screw extrusion type evaporation coking device, 5-an oil phase evaporation product outlet, a 6-distillate oil gas phase outlet, 7-a separating tank, 8-a heat exchanger, 9-a reduced pressure distillation zone, 10-a coking zone, 11-a coke outlet, 12-a feeding pipeline and 13-a feeding hole.
Detailed Description
The present invention will be described in further detail with reference to specific examples, which are provided for illustrative purposes only, and are not intended to be limiting, and the scope of the present invention should not be limited thereby.
A coal hydrogenation residue coking system comprises a feeding pipeline 12, a hydrogenation reactor 1 and a hot high-pressure separator 2, wherein the feeding pipeline is connected to an inlet of the hydrogenation reactor, an outlet of the hydrogenation reactor is connected with an inlet of the hot high-pressure separator, a gas phase outlet is formed in the top of the hot high-pressure separator, and a slurry outlet is formed in the bottom of the hot high-pressure separator. The innovation of the coal hydrogenation residue coking system is as follows: the slurry outlet at the bottom of the thermal high-pressure separator is connected to a feed inlet 13 of a screw extrusion type evaporation coking device 4 through a solvent pump 3, the screw extrusion type evaporation coking device is provided with a reduced pressure distillation area 9 and a coking area 10, the reduced pressure distillation area is provided with an oil phase evaporation product outlet 5, the oil phase evaporation product outlet is connected to a separation tank 7 through an evaporation product pipeline through a heat exchanger 8, and the coking area is provided with a distillate oil gas phase outlet 6 and a coke outlet 11.
The separating tank connected with the reduced pressure distillation area is connected with a vacuum pump, and the reduced pressure distillation area is under negative pressure with the pressure of 0.01-0.5 bara. A separation zone 14 is provided between the reduced pressure distillation zone and the coking zone, and the separation zone is provided with a material port for material to pass in and out without affecting the rotation of the screw.
The screw extrusion type evaporation coking device adopts a double-screw extruder. The feed inlet of the screw extrusion type evaporative coking device is arranged on the bottom surface of the shell of the screw extrusion type evaporative coking device; the reduced pressure distillation area is provided with an oil phase evaporation product outlet which is arranged at the upper part of the shell of the screw extrusion type evaporation coking device.
The working principle of the coal hydrogenation residue coking system is as follows:
carrying out reduced pressure distillation on the coal hydrogenation residue in a screw extrusion type evaporation coking device, extracting wax oil in the process, continuously coking the residual slurry in an extruder, and generating part of light distillate oil through condensation reaction in the coking process and recovering the light distillate oil; during the process of carrying out reduced pressure distillation and coking on the coal hydrogenation residue, materials can continuously move forward in the extruder by a screw in the extruder, the extruder conveys slurry to pass through a reduced pressure distillation area and a coking area of the device, the viscosity of the residual materials is continuously increased along with continuous gasification of a liquid phase, in the process, firstly, volatile components (mainly wax oil components) are extracted from the slurry in the reduced pressure distillation area, and then the residue passes through the coking area, wherein the volatile components are subjected to thermal cracking reaction to generate coking distillate oil, and the distillate oil is also extracted.
The double screw extruder can be operated under the negative pressure environment and has the function of gas or steam extraction, the difficulty of oil-solid separation of hydrogenation residues exists for a long time since the coal hydrogenation process reaches the industrial scale, the recommended pressure in the reduced pressure distillation zone of the double screw extruder is 0.01-0.5bara (optimal value: 0.05-0.1bara), the pressure in the reduced pressure distillation zone of the screw extruder is kept constant negative pressure and the temperature is kept constant from the slurry inlet to the zone outlet, the pressure is kept constant and is 250-, the slurry is basically composed of a liquid phase of asphaltenes/colloids, and solids such as ash and catalysts in coal.
A separation zone is arranged between the reduced pressure distillation zone and the coking zone, a material port is arranged in the separation zone, the reduced pressure distillation zone and the coking zone are properly separated by a vacuum zone and an atmospheric zone, but the material transmission needs to be ensured, the operation pressure of the coking zone is normal pressure, the temperature is 400-. Or further hydrogenation treatment to produce gasoline and diesel oil. In order to prevent carbon deposition on the screw in the coking area of coke and influence the transmission efficiency, the screw can be made of metal materials with smooth surfaces, and a high-pressure water gun is arranged in the screw in the coking area to remove the carbon deposition regularly.
Although the embodiments of the present invention and the accompanying drawings have been disclosed for illustrative purposes, those skilled in the art will appreciate that various substitutions, alterations, and modifications are possible without departing from the spirit and scope of the invention and the appended claims, and thus the scope of the invention is not limited to the embodiments and drawings disclosed.
Claims (5)
1. The utility model provides a coal hydrogenation residue coking system, includes feedstock line, hydrogenation ware, hot high pressure separator, and feedstock line is connected to the hydrogenation ware import, and the hydrogenation ware exit linkage hot high pressure separator import, hot high pressure separator top set up the gas phase export, and the bottom is the thick liquids export, its characterized in that: the slurry outlet at the bottom of the thermal high-pressure separator is connected to a feed inlet of a screw extrusion type evaporation coking device through a solvent pump, the screw extrusion type evaporation coking device is provided with a reduced pressure distillation area and a coking area, the reduced pressure distillation area is provided with an oil phase evaporation product outlet, the oil phase evaporation product outlet is connected to a separation tank through an evaporation product pipeline, and the coking area is provided with a distillate oil gas phase outlet and a coke outlet.
2. The coal hydrogenation residue coking system of claim 1, characterized in that: the separating tank connected with the reduced pressure distillation area is connected with a vacuum pump, and the reduced pressure distillation area is under negative pressure with the pressure of 0.01-0.5 bara.
3. The coal hydrogenation residue coking system of claim 1, characterized in that: a separation area is arranged between the reduced pressure distillation area and the coking area, and a material port is formed in the separation area.
4. The coal hydrogenation residue coking system of claim 1, characterized in that: the screw extrusion type evaporation coking device adopts a double-screw extruder.
5. The coal hydrogenation residue coking system of claim 1, characterized in that: the feed inlet of the screw extrusion type evaporative coking device is arranged on the bottom surface of the shell of the screw extrusion type evaporative coking device; the reduced pressure distillation area is provided with an oil phase evaporation product outlet which is arranged at the upper part of the shell of the screw extrusion type evaporation coking device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021555249.6U CN212687968U (en) | 2020-07-31 | 2020-07-31 | Coal hydrogenation residue coking system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021555249.6U CN212687968U (en) | 2020-07-31 | 2020-07-31 | Coal hydrogenation residue coking system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212687968U true CN212687968U (en) | 2021-03-12 |
Family
ID=74900306
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202021555249.6U Active CN212687968U (en) | 2020-07-31 | 2020-07-31 | Coal hydrogenation residue coking system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN212687968U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11920099B2 (en) | 2021-11-23 | 2024-03-05 | Saudi Arabian Oil Company | Extruder systems and processes for production of petroleum coke |
| US11959022B2 (en) | 2021-11-23 | 2024-04-16 | Saudi Arabian Oil Company | Extruder systems and processes for production of petroleum coke and mesophase pitch |
-
2020
- 2020-07-31 CN CN202021555249.6U patent/CN212687968U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11920099B2 (en) | 2021-11-23 | 2024-03-05 | Saudi Arabian Oil Company | Extruder systems and processes for production of petroleum coke |
| US11959022B2 (en) | 2021-11-23 | 2024-04-16 | Saudi Arabian Oil Company | Extruder systems and processes for production of petroleum coke and mesophase pitch |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN212687968U (en) | Coal hydrogenation residue coking system | |
| US9068126B2 (en) | Methods for deoxygenating biomass-derived pyrolysis oil | |
| US10010839B2 (en) | Process to upgrade highly waxy crude oil by hot pressurized water | |
| CN106701178B (en) | A kind of coal tar suspension bed method for hydrogen cracking | |
| EP1707614A1 (en) | Thermal or catalytic cracking process for hydrocarbon feedstocks and corresponding system | |
| US20090077888A1 (en) | Process and device for gasification of crude glycerol | |
| US4584060A (en) | Low temperature carbonization process for coal hydrogenation residues | |
| CN103484159B (en) | Matching technology method for optimizing feeding of coal tar suspended bed hydrocracker | |
| CN109111950B (en) | Method for producing liquid fuel by hydrogenating full-fraction tar | |
| US4477334A (en) | Thermal cracking of heavy hydrocarbon oils | |
| JPH08269459A (en) | Coal liquefaction method | |
| CN203559012U (en) | Coal tar treatment system | |
| CN205152158U (en) | Coal tar suspension bed hydrocracking unit | |
| JP2530593B2 (en) | Continuous thermal hydrogenation and conversion process for carbonaceous feedstock containing solids | |
| WO2010150272A1 (en) | System and method for material recycling and resource recovery | |
| CN102453511B (en) | Method for preparing synthesis gas by coupled processing of coal and heavy oil | |
| US4583995A (en) | Method of producing synthesis gas | |
| WO1980001281A1 (en) | Coal liquefaction-gasification process including reforming of naphtha product | |
| CN109652121B (en) | Undoped full-fraction ethylene tar delay coking equipment | |
| US4226698A (en) | Ash removal and synthesis gas generation from heavy oils produced by coal hydrogenation | |
| CN1011416B (en) | Coking technology of oil residues with double feeding system | |
| CA1130740A (en) | Converting coal with gaseous and liquid fuels | |
| CN113999690B (en) | Device and method for pyrolysis treatment of coal tar fluidized bed | |
| CA1239105A (en) | Method of recovering volatile oils from hydrogenation residues of heavy oils, very heavy oils, bitumen, tar, or the like | |
| JPH047399B2 (en) |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |