CN110373224B - Method for resisting heating and coking of heavy distillate oil - Google Patents
Method for resisting heating and coking of heavy distillate oil Download PDFInfo
- Publication number
- CN110373224B CN110373224B CN201910624291.4A CN201910624291A CN110373224B CN 110373224 B CN110373224 B CN 110373224B CN 201910624291 A CN201910624291 A CN 201910624291A CN 110373224 B CN110373224 B CN 110373224B
- Authority
- CN
- China
- Prior art keywords
- furnace
- tower
- vacuum
- distillate oil
- atmospheric tower
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to the technical field of coal chemical industry, and discloses a method for resisting heating and coking of heavy distillate oil. The method is implemented in a system comprising an atmospheric tower, a vacuum furnace and a vacuum tower, wherein the atmospheric tower, the vacuum furnace and the vacuum tower are sequentially communicated along the material direction, the vacuum furnace is provided with a plurality of independent hearths, and the method specifically comprises the following steps: (1) sending light, medium and heavy distillate oil from a coal liquefaction device into an atmospheric tower for distillation, wherein the operating pressure of the atmospheric tower is 0.1-0.9 MPa; (2) sending heavy distillate oil from the bottom of the atmospheric tower into any hearth of the vacuum furnace to carry out single-hearth heating; (3) the material from the vacuum furnace is sent to a vacuum tower for fractionation. The method solves the problem that the heavy distillate oil at the bottom of the atmospheric tower blocks a pipeline due to coking, and prolongs the operation periods of the vacuum furnace and the vacuum tower.
Description
Technical Field
The invention relates to the technical field of coal chemical industry, in particular to a method for resisting heating and coking of heavy distillate oil.
Background
The coal chemical industry field using coal powder as raw material, especially the direct coal liquefaction system, first prepares the raw material coal, catalyst and hydrogen supply solvent from hydrogenation stabilizer into oil coal slurry, then replenishes liquid sulfur, reacts part of the oil coal slurry and hydrogen under the action of high temperature, high pressure and catalyst to generate liquefied oil, one part of the gas component rich in hydrogen is recycled, and the other part of sulfur-containing gas is sent to the desulfurizer. In the fractionation part, the liquefied oil generated by the reaction is firstly fractionated by an atmospheric tower to obtain flash gas and oil products, and the residual heavy distillate oil containing solids is heated by a decompression furnace again, decompressed by a decompression valve and then enters a decompression tower for fractionation. The heavy distillate oil containing solid at the bottom of the atmospheric tower has high temperature, high solid content and high viscosity, is rich in unreacted coal dust, iron in a catalyst and ash in the coal dust, has very complex components, and is heated by a decompression furnace to raise the temperature to 390-. In the heating process, after the materials in the furnace tube exceed a certain temperature limit, a thermal cracking condensation reaction is carried out to produce coking, and a coking material is generated on the inner wall of the furnace tube; secondly, because the length of a single pipe of the pressure reducing furnace can reach 480 meters, the phenomenon of gas-liquid-solid three-phase layering occurs because the flow patterns of materials at the inlet and the outlet of the furnace are different due to overlong pipelines. The flow rate is low, the boundary is thick, heat cannot be taken away, and coking is accelerated. In addition, the materials in the coal liquefaction decompression furnace contain more pre-asphaltene and asphaltene, the coking tendency is more serious than that of other materials, the materials are easy to coke, and the local heating is too large due to the reasons of production adjustment, low material flow rate in a pipeline and the like, so that the furnace tube is easy to coke.
The existing coal liquefaction decompression furnace is designed into a double-sided radiation heating furnace, which is divided into two hearths AB, and each hearth is provided with two furnace tubes. According to the load adjustment of the coal liquefaction decompression furnace, the feeding range of the decompression furnace is 200-400t/h, and the flow velocity range of a single furnace tube is calculated to be 1-2 m/s. Under the working condition, coking is serious in the furnace tube, so that the decompression furnace is difficult to normally operate frequently, the flow rate is low, the pressure difference is high, and the continuous operation time of the decompression furnace is at most 3 months. Most seriously, once the furnace tube of the pressure reducing furnace is coked, the furnace tube needs to be cleaned after being divided, the damage to the furnace tube is large, and the workload is large. The pipe diameter from the outlet of the existing pressure reducing furnace to the main pipe of the pressure reducing tower is DN400, the actual flow rate in the furnace pipe of the heating furnace is 0.5-1m/s under the actual operation load, the coking materials in the inner wall of the pipeline are serious, and when the production device is started or stopped or the temperature is raised or lowered, the coking materials on the inner wall of the pipeline fall off into the pipeline and are carried to a downstream pressure reducing tower along with the materials, the bottom suction outlet of the pressure reducing tower and the inlet and outlet of a bottom pump of the pressure reducing tower are blocked, the load of the device is influenced, and the device must be stopped. When in coke cleaning, the mechanical coke cleaning gun head is difficult to capture the coking part in the pipeline because the pipe diameter and the length of the furnace outlet pipeline are large. The factors seriously restrict the high-load long-period stable operation of the device.
Disclosure of Invention
The invention aims to overcome the problem that heavy distillate oil at the bottom of the atmospheric tower is coked in a vacuum furnace and an outlet pipeline in the heating and temperature rising process in the prior art, and provides a method for resisting heating and coking of the heavy distillate oil.
In order to achieve the above object, the present invention provides a method for resisting heating and coking of heavy distillate oil, which is implemented in a system comprising an atmospheric tower, a vacuum furnace and a vacuum tower, wherein the atmospheric tower, the vacuum furnace and the vacuum tower are sequentially communicated along the material direction, the vacuum furnace is provided with a plurality of independent hearths, and the method specifically comprises the following steps:
(1) sending light, medium and heavy distillate oil from a coal liquefaction device into an atmospheric tower for distillation, wherein the operating pressure of the atmospheric tower is 0.1-0.9 MPa;
(2) sending heavy distillate oil from the bottom of the atmospheric tower into any hearth of the vacuum furnace to carry out single-hearth heating;
(3) the material from the vacuum furnace is sent to a vacuum tower for fractionation.
Preferably, the decompression furnace has 2 independent hearths.
Preferably, the outlet pipe of the decompression furnace has a pipe diameter of DN 200-300.
In the method, light, medium and heavy distillate oil from a coal liquefaction device is sent to the atmospheric tower for distillation, so that the content of light components in the heavy distillate oil at the bottom of the atmospheric tower is reduced; the heavy distillate oil from the atmospheric tower enters one hearth of the vacuum furnace to be heated, so that the flow rate of materials in the furnace is increased, the phenomenon of gas-liquid-solid three-phase layering of the materials in the vacuum furnace is improved, and the operation time of the vacuum furnace is prolonged; furthermore, the vacuum furnace adopts an outlet pipe with a small pipe diameter, so that the retention time and coking rate of materials in the pipeline are reduced, the problem that the pipeline is blocked by coking of heavy distillate oil at the bottom of the atmospheric tower is solved, and the operation period of the system is prolonged.
Drawings
FIG. 1 is a schematic flow chart of the method of the present invention.
Description of the reference numerals
1 atmospheric tower 2 vacuum furnace
3 decompression tower 4 first furnace inlet regulating valve
5 second furnace inlet regulating valve 6 third furnace inlet regulating valve
7 fourth furnace inlet regulating valve 8A furnace outlet ball valve
9B furnace outlet ball valve 10 decompression furnace outlet cut-off valve
11 pressure reducing tower inlet pressure reducing valve 12 normal outward-feeding pump
13-normal two-external-feeding pump and 14-normal three-external-feeding pump
15 minus one external pump and 16 minus two external pumps
17 subtract three external pump 18 and subtract bottom pump
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
In the present invention, the use of directional terms such as "upper" and "lower" generally means upper and lower as shown in the drawings without being described to the contrary.
The invention provides a method for resisting heating and coking of heavy distillate oil, which is implemented in a system comprising an atmospheric tower 1, a vacuum furnace 2 and a vacuum tower 3, wherein the atmospheric tower 1, the vacuum furnace 2 and the vacuum tower 3 are sequentially communicated along the material direction, the vacuum furnace 2 is provided with a plurality of independent hearths, and the method specifically comprises the following steps:
(1) sending light, medium and heavy distillate oil from a coal liquefaction device into an atmospheric tower 1 for distillation, wherein the operating pressure of the atmospheric tower 1 is 0.1-0.9 MPa;
(2) sending heavy distillate oil from the bottom of the atmospheric tower 1 into any hearth of the vacuum furnace 2 for single hearth heating;
(3) the material from the vacuum furnace 2 is sent to the vacuum tower 3 for fractionation.
In the method, light, medium and heavy distillate oil from a coal liquefaction device is sent to the atmospheric tower 1 for distillation, so that the content of light components in the heavy distillate oil at the bottom of the atmospheric tower is reduced; the heavy distillate oil from the atmospheric tower 1 enters one hearth of the vacuum furnace 2 to be heated and heated, the single hearth operation improves the flow rate of materials in the furnace, improves the phenomenon of gas-liquid-solid three-phase layering of the materials in the vacuum furnace, and prolongs the operation time of the vacuum furnace; furthermore, the vacuum furnace 2 adopts an outlet pipe with a small pipe diameter, so that the retention time and coking rate of materials in the pipeline are reduced, the problem that the pipeline is blocked by coking of heavy distillate oil at the bottom of the atmospheric tower is solved, and the operation period of the system is prolonged.
In a preferred embodiment, the decompression furnace 2 has 2 independent hearths, namely hearth a and hearth B.
But every furnace individual operation compares with the same flue operation of original double-furnace sharing, and single-furnace operation has improved and has come from the velocity of flow of the heavy distillate oil at the bottom of the atmospheric tower 1's atmospheric tower has improved heavy distillate oil and has been in the phenomenon of the layering of gas liquid solid three-phase in the boiler tube of decompression furnace 2 to reduce heavy distillate oil and coke at the boiler tube inner wall, avoid blockking up follow-up equipment, increased simultaneously the stability of system has avoided leading to because of the intensification cooling that the adjustment load brought coking in the boiler tube of decompression furnace 2.
The 2 independent hearths can be operated according to single hearth operation, so that one hearth can be used, and the operation time of the decompression furnace 2 is prolonged. The materials in the standby furnace tube need to be washed clean, the oil is filled for standby, and the hearth inlet and outlet valves need to be closed to realize isolation. And when the single hearth operates, the flow velocity of the materials in the furnace tube is increased to 2-4m/s from the flow velocity of 1-2m/s of the original double hearths.
Further, the system implemented by the method further comprises a first furnace inlet regulating valve 4, a second furnace inlet regulating valve 5, a third furnace inlet regulating valve 6, a fourth furnace inlet regulating valve 7, a furnace A outlet ball valve 8, a furnace B outlet ball valve 9, a pressure reducing furnace outlet cut-off valve 10, a pressure reducing tower inlet pressure reducing valve 11, a normal one outward-feeding pump 12, a normal two outward-feeding pump 13, a normal three outward-feeding pump 14, a minus one outward-feeding pump 15, a minus two outward-feeding pump 16, a minus three outward-feeding pump 17 and a bottom reducing pump 18.
The first furnace inlet regulating valve 4, the second furnace inlet regulating valve 5, the third furnace inlet regulating valve 6 and the fourth furnace inlet regulating valve 7 are used for regulating the flow of the atmospheric tower bottom heavy distillate oil entering the vacuum furnace 2; the furnace A outlet ball valve 8 and the furnace B outlet ball valve 9 respectively control whether the materials from the hearth A and the hearth B flow or not; the pressure reducing furnace outlet cut-off valve 10 is used for controlling whether the materials in the main outlet pipeline of the pressure reducing furnace 2 flow or not, and the pressure reducing tower inlet pressure reducing valve 11 is used for carrying out pressure reduction treatment on the materials from the pressure reducing furnace 2; the normal-two external feeding pump 12, the normal-three external feeding pump 13 and the normal-three external feeding pump 14 are used for conveying the side-cut oil of the atmospheric tower 1; the minus one external feed pump 15, the minus three external feed pump 16 and the minus three external feed pump 17 are used for conveying the side-cut oil of the vacuum tower 3; the bottom-reducing pump 18 is used for conveying materials extracted from the bottom of the decompression tower 3.
Preferably, the outlet pipe of the decompression furnace 2 has a pipe diameter of DN 200-300.
The outlet pipe diameter of the decompression furnace 2 in the prior double-hearth operation is DN400, and the residence time of the material in the pipeline is reduced by reducing the outlet pipe diameter of the decompression furnace 2, so that the coking rate is reduced, and the blockage of the decompression tower 3 is avoided.
Furthermore, the outlet pipe of the decompression furnace 2 is a large-radius bent pipe which is horizontally arranged, so that erosion of the outlet pipeline caused by the three-phase material which contains solid particles and is in a mixed phase flow in the decompression furnace 2 can be prevented.
FIG. 1 is a schematic flow diagram of the process of the present invention. Referring to fig. 1, light distillate oil, middle distillate oil and heavy distillate oil from a coal liquefaction device enter the atmospheric tower 1 from the top, middle and bottom of the atmospheric tower 1 respectively for distillation, the operating pressure of the atmospheric tower 1 is reduced from 0.8MPa to 0.1-0.2MPa, the flash evaporation proportion of gas and light oil in an oil phase is increased, so that the light component content in heavy oil at the bottom of the atmospheric tower is reduced and the temperature of the heavy oil is reduced, atmospheric tower top gas obtained by reduced pressure distillation is sent to a downstream light hydrocarbon recovery device, normal linear and normal three linear side oil are sent to a downstream hydrogenation stabilizing device through the normal linear and normal two external pumps 12, 13 and 14, and the atmospheric tower bottom heavy oil enters a hearth a or a hearth B of the reduced pressure furnace 2 through the first furnace inlet regulating valve 4, the second furnace inlet regulating valve 5, the third furnace inlet regulating valve 6 and the fourth furnace inlet regulating valve 7 for heating and temperature rise The single hearth operation improves the flow velocity of materials in the furnace, and improves the phenomenon of gas-liquid-solid three-phase layering of the materials in the decompression furnace 2; furthermore, the outlet pipe of the vacuum furnace 2 adopts a large-radius bent pipe with a small pipe diameter and arranged in a horizontal pipe, so that the retention time and coking rate of the material in the pipeline are reduced, and the outlet pipe is prevented from being eroded by the material, thereby solving the problem that the pipeline is blocked by coking of heavy oil at the bottom of the normal pressure tower, and prolonging the operation period of the system. The method comprises the following steps that materials from a decompression furnace 2 pass through a furnace A outlet ball valve 8 or a furnace B outlet ball valve 9, a decompression furnace outlet cut-off valve 10, are decompressed by a decompression tower inlet decompression valve 11 and then enter a decompression tower 3 for fractionation, decompression tower top gas obtained by fractionation is sent to a downstream light hydrocarbon recovery device, first-line and second-line side line extracted oil is sent to a downstream hydrogenation stabilizing device through a first-line and second-line side line extracted oil delivery pump 15 and a second-line and external delivery pump 16, part of the third-line side line extracted oil flows back to the decompression tower 3, the rest part of the third-line side line extracted oil returns to the decompression furnace 2 through a third-line and external delivery pump 17, part of the materials from the bottom of the decompression tower 3 flows back to the decompression tower 3, and the rest of the third-line extracted oil flows back to.
Preferably, the temperature of the heavy oil at the bottom of the atmospheric tower obtained after distillation in the atmospheric tower 1 is 300-400 ℃, and the temperature of the material obtained after heating in the vacuum furnace 2 is 390-420 ℃.
The present invention will be described in detail by way of examples, but the scope of the present invention is not limited thereto.
Example 1
Light distillate oil, middle distillate oil and heavy distillate oil from a coal liquefaction device respectively enter the atmospheric tower 1 from the top, the middle and the bottom of the atmospheric tower 1 for distillation, wherein the operating pressure of the atmospheric tower 1 is 0.16 MPa; sending heavy distillate oil from the bottom of the atmospheric tower 1 into a hearth A of a vacuum furnace 2 to be heated to 410 ℃; the material from the vacuum furnace 2 is sent to the vacuum tower 3 for fractionation.
Example 2
Light distillate oil, middle distillate oil and heavy distillate oil from a coal liquefaction device respectively enter the atmospheric tower 1 from the top, the middle and the bottom of the atmospheric tower 1 for reduced pressure distillation, wherein the operating pressure of the atmospheric tower 1 is 0.18 MPa; sending heavy distillate oil from the bottom of the atmospheric tower 1 to a hearth A of a vacuum furnace 2 to heat and raise the temperature to 415 ℃; the material from the vacuum furnace 2 is sent to the vacuum tower 3 for fractionation.
Example 3
Light distillate oil, middle distillate oil and heavy distillate oil from a coal liquefaction device respectively enter the atmospheric tower 1 from the top, the middle and the bottom of the atmospheric tower 1 for reduced pressure distillation, wherein the operating pressure of the atmospheric tower 1 is 0.12 MPa; sending heavy distillate oil from the bottom of the atmospheric tower 1 to a hearth A of a vacuum furnace 2 to heat to 405 ℃; the material from the vacuum furnace 2 is sent to the vacuum tower 3 for fractionation.
Comparative example 1
The atmospheric bottom heavy distillate from the atmospheric tower 1 was heated and fractionated as in example 1, except that the vacuum furnace 2 was a double hearth furnace.
Comparative example 2
The atmospheric bottom heavy distillate from the atmospheric tower 1 was heated and fractionated as in example 1 except that the atmospheric tower 1 was not distilled under reduced pressure and the operating pressure was 0.8 MPa.
Test example
The operation cycle of the systems of examples 1 to 3 and comparative examples 1 to 2 was recorded, and whether or not coking occurred in the line from the outlet of the vacuum furnace 2 to the vacuum tower 3 was observed, and the results are shown in Table 1.
TABLE 1
| Item | Operating cycle (moon) | Whether or not coking occurs |
| Example 1 | 15 | Whether or not |
| Example 2 | 14 | Whether or not |
| Example 3 | 14 | Whether or not |
| Comparative example 1 | 6 | Coking of heavy metals |
| Comparative example 2 | 3 | Coking of heavy metals |
As can be seen from the results in Table 1, the system and the method of the invention can reduce the coking of the furnace tube of the vacuum furnace and prolong the operation period of the system.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (2)
1. The method for resisting heating coking of heavy distillate oil is characterized by being implemented in a system comprising an atmospheric tower (1), a vacuum furnace (2) and a vacuum tower (3), wherein the atmospheric tower (1), the vacuum furnace (2) and the vacuum tower (3) are sequentially communicated along the material direction, the vacuum furnace (2) is provided with a plurality of independent hearths, and the method specifically comprises the following steps:
(1) sending light, medium and heavy distillate oil from a coal liquefaction device into an atmospheric tower (1) for distillation, wherein the operating pressure of the atmospheric tower (1) is 0.1-0.9 MPa;
(2) sending heavy distillate oil from the bottom of the atmospheric tower (1) into any hearth of the vacuum furnace (2) for single-hearth heating, wherein the flow velocity of the heavy distillate oil in the hearth is 2-4m/s, and the pipe diameter of an outlet pipe of the vacuum furnace (2) is DN 200-300;
(3) the material from the vacuum furnace (2) is sent to a vacuum tower (3) for fractionation.
2. The method according to claim 1, characterized in that the decompression furnace (2) has 2 independent hearths.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910624291.4A CN110373224B (en) | 2019-07-11 | 2019-07-11 | Method for resisting heating and coking of heavy distillate oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910624291.4A CN110373224B (en) | 2019-07-11 | 2019-07-11 | Method for resisting heating and coking of heavy distillate oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110373224A CN110373224A (en) | 2019-10-25 |
| CN110373224B true CN110373224B (en) | 2021-04-23 |
Family
ID=68252788
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910624291.4A Active CN110373224B (en) | 2019-07-11 | 2019-07-11 | Method for resisting heating and coking of heavy distillate oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110373224B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114437755A (en) * | 2020-11-04 | 2022-05-06 | 山西潞安煤基清洁能源有限责任公司 | Coal-to-liquid product delivery system |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203284371U (en) * | 2013-03-27 | 2013-11-13 | 中国石油天然气股份有限公司 | Double-sided radiant tube type heating furnace |
| CN104896926B (en) * | 2015-06-01 | 2016-11-16 | 北京中科诚毅科技发展有限公司 | The heating furnace of a kind of multiple hearth structure and method for designing thereof and purposes |
| CN109181744A (en) * | 2018-11-14 | 2019-01-11 | 胜帮科技股份有限公司 | One kind is containing solid heavy oil reduced pressure distillation process device and method |
| CN109504421B (en) * | 2018-11-28 | 2020-12-22 | 洛阳瑞华新能源技术发展有限公司 | Method for extracting distilled oil from heavy oil-containing hydrocarbon stream by deep vaporization |
-
2019
- 2019-07-11 CN CN201910624291.4A patent/CN110373224B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN110373224A (en) | 2019-10-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101289624B (en) | Process for producing moderate temperature modified bitumen by continuously pressurizing and hot-polymerizing at two stages connected in series | |
| CN110373224B (en) | Method for resisting heating and coking of heavy distillate oil | |
| CN110589880A (en) | Vanadium removal method for titanium tetrachloride refined organic matter | |
| CN109052459B (en) | For preparing TiCl4Chlorination furnace and furnace temperature control method thereof | |
| CN103254919B (en) | Technique and device for preventing deposition and blockage of tar residues of tar system | |
| CN102994162A (en) | Circulating fluidized bed gasifier system and starting method thereof | |
| CN212687968U (en) | Coal hydrogenation residue coking system | |
| CN110229689B (en) | Distillation device and method for solid-containing raw oil | |
| US20170073594A1 (en) | Gasification system | |
| CN108913202B (en) | Skid-mounted decompression system | |
| WO2016176983A1 (en) | Hydrogenation process temperature control method, and design method therefor and use thereof | |
| CN212644553U (en) | Coke oven crude gas riser pipe configuration waste heat recovery steam generation device | |
| CN103361112B (en) | Device for blending catalytic slurry oil in delayed coking technology and method thereof | |
| CN109181744A (en) | One kind is containing solid heavy oil reduced pressure distillation process device and method | |
| CN109971513B (en) | Multi-stage cooling process and device for coke oven crude gas | |
| CN210473953U (en) | Liquid phase hydrogenation hydrogen dissolving test device | |
| CN108342219B (en) | Heavy oil and oil coal hydrogenation process and method for processing self-produced heavy distillate oil thereof | |
| CN204644283U (en) | Reclaim the device of coker emptying tower top gas | |
| CN105087065B (en) | Pyrolysis gasoline central fraction hydrogenation device and method thereof | |
| JP2017520726A (en) | System and method for handling heavy oil residues | |
| CN205420292U (en) | Atmospheric and vacuum unit triple tops waste gas recovery recycles device | |
| CN206375858U (en) | Solvent deasphalting process unit of inferior heavy oil | |
| CN113004938A (en) | Oil slurry safe discharge system and safe discharge method of slurry bed hydrocracking device | |
| CN215335812U (en) | Coke drum special valve system with steam injection and flow stabilization functions | |
| CN204848770U (en) | Reduce low recycle ratio coker of coke yield |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |