CN112592727A - Method for recovering oil product by coal-to-liquid circulating gas decarburization unit - Google Patents
Method for recovering oil product by coal-to-liquid circulating gas decarburization unit Download PDFInfo
- Publication number
- CN112592727A CN112592727A CN202011163751.7A CN202011163751A CN112592727A CN 112592727 A CN112592727 A CN 112592727A CN 202011163751 A CN202011163751 A CN 202011163751A CN 112592727 A CN112592727 A CN 112592727A
- Authority
- CN
- China
- Prior art keywords
- circulating gas
- oil
- coal
- separator
- decarburization unit
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
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
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a method for recovering oil products by a coal-to-liquid circulating gas decarburization unit, wherein the coal-to-liquid circulating gas decarburization unit enables circulating gas from a compressor to enter a purified gas system after passing through a water washing tower and an absorption tower; the method is characterized in that: the circulating gas from the compressor is subjected to oil-gas separation by a separator and then enters a coal-to-liquid circulating gas decarburization unit; leading the circulating gas passing through the separator to a coal-to-liquid circulating gas decarburization unit; the oil product passing through the separator is led to an oil synthesis unit for recovery. The method has the advantages of high recovery rate, less equipment investment and simple operation, and solves the problem that the oil product is carried in the circulating gas of the coal-to-liquid decarbonization unit.
Description
Technical Field
The invention relates to the field of energy conservation and environmental protection, in particular to a method for recovering oil by a coal-to-liquid circulating gas decarburization unit.
Background
The process for preparing oil from coal is to indirectly synthesize liquid fuel by using coal as raw material, and H is used in reaction2And CO inWhile hydrocarbon products are generated on the original catalyst, water is generated during the reaction process, and the water and CO carry out water gas shift reaction to generate a large amount of CO2. Thus, after separation of the products of the gas leaving the synthesis reactor, the remaining tail gas must be freed of CO before it can be recycled2. But in the removal of CO2Meanwhile, the gas can contain oil products in a synthesis section, so that not only is the product loss in the synthesis section caused, but also the loss of the solvent in the decarburization unit and the corrosion of equipment are caused when the oil products enter the decarburization unit, so that the circulating gas is subjected to CO removal in the decarburization unit2Before the oil product is recovered.
In order to solve the problem, the invention provides a process for removing CO from coal-to-liquids circulating gas2Before, the oil is recovered.
Disclosure of Invention
1. The technical problem to be solved is as follows:
aiming at the technical problem, the invention provides a method for recovering oil by a coal-to-liquid circulating gas decarburization unit, which is characterized in that a separation device is additionally arranged on the decarburization unit, the circulating gas enters the decarburization unit and enters the separation device for oil-gas separation, the separation device is provided with a liquid level meter, when the liquid level reaches a set height, an oil pump is started, the separated oil is returned to a synthesis unit for recovery, an online analyzer is arranged on a recovery pipeline, when the oil concentration is less than 90%, the oil pump is closed, and the circulating gas after oil separation enters a water scrubber for water washing.
2. The technical scheme is as follows:
a method for recycling oil products by a coal-to-liquid circulating gas decarburization unit is characterized in that the coal-to-liquid circulating gas decarburization unit enables circulating gas from a compressor to enter a purified gas system after passing through a water washing tower and an absorption tower; the method is characterized in that: the circulating gas from the compressor is subjected to oil-gas separation by a separator and then enters a coal-to-liquid circulating gas decarburization unit; leading the circulating gas passing through the separator to a coal-to-liquid circulating gas decarburization unit; the oil product passing through the separator is led to an oil synthesis unit for recovery.
Further, the oil passing through the separator is pumped out by an oil pump.
Furthermore, the oil product is recycled after passing through the condensing device.
Further, the temperature in the separator is controlled within the range of 30-110 ℃.
Further, the operation pressure in the separator is 0.1-5 MPa.
Further, a liquid level meter is arranged in the separator, and when the liquid level in the separator reaches a preset height, an oil pump is started to pump oil.
Further, the circulating gas from the compressor firstly enters the separator after passing through the on-line analysis equipment, and when the oil concentration is less than 90%, the oil pump is closed.
3. Has the advantages that:
the method for recovering the oil product in the circulating gas has the advantages of high recovery rate, less equipment investment and simple operation, and solves the problem that the oil product is carried in the circulating gas of the coal oil decarburization unit.
Drawings
FIG. 1 is a schematic view of the apparatus of the present invention.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings.
As shown in the attached figure 1, in the method for recovering the oil product by the coal-to-liquid circulating gas decarburization unit, the circulating gas from a compressor enters a purified gas system or a regeneration system after passing through a water scrubber 2 and an absorption tower 4 by the coal-to-liquid circulating gas decarburization unit; the method is characterized in that: circulating gas from a compressor firstly passes through a separator 1 for oil-gas separation and then enters a coal-to-liquid circulating gas decarburization unit; leading the circulating gas passing through the separator to a coal-to-liquid circulating gas decarburization unit; the oil product passing through the separator is led to an oil synthesis unit for recovery.
Further, the oil passing through the separator is pumped out by an oil pump 3.
Furthermore, the oil product is recycled after passing through the condensing device.
Further, the temperature in the separator is controlled within the range of 30-110 ℃.
Further, the operation pressure in the separator is 0.1-5 MPa.
Further, a liquid level meter is arranged in the separator, and when the liquid level in the separator reaches a preset height, an oil pump is started to pump oil.
Further, the circulating gas from the compressor firstly passes through an online analysis device, and when the oil concentration is less than 90%, the oil pump is closed.
The specific embodiment is as follows:
example 1:
an oil separator is arranged in front of the water scrubber, the structure size is phi 6000 multiplied 14000, the total gas quantity before the circulating gas enters the decarburization unit is 29000Kmol/h, the main components are an oxidation tower, hydrogen, hydrocarbons, carbon dioxide and water, the concentration of the oil is about 6 percent, the operation pressure is 2.7Mpa, and the gas temperature is 40 ℃. The circulating gas enters a separator for oil product separation, and the oil product concentration in the circulating gas is reduced to 0.5 percent after separation. The recovered oil is returned to the synthesis unit, so that the load of the yield decarburization unit of the device is reduced, and meanwhile, the loss of the oil brought into the decarburization system to the solvent of the unit is reduced.
Example 2:
an oil separator is arranged in front of the water scrubber, the structural size is phi 3600 multiplied by 8000, the total gas quantity before the circulating gas enters the decarburization unit is 10000Kmol/h, the main components are an oxidation tower, hydrogen, hydrocarbons, carbon dioxide and water, the concentration of the oil is about 9 percent, the operating pressure is 3.5Mpa, the gas temperature is 75 ℃, the circulating gas enters the separator for separation, and the concentration of the oil in the circulating gas is reduced to 0.9 percent after separation.
Example 3:
an oil separator is arranged in front of the water scrubber, the structural size is phi 4000 multiplied 8000, the total gas quantity before the circulating gas enters the decarburization unit is 13600Kmol/h, the main components are an oxidation tower, hydrogen, hydrocarbons, carbon dioxide and water, the concentration of the oil is about 7%, the operating pressure is 3.45Mpa, the gas temperature is 77 ℃, the circulating gas enters the separator for separation, and the concentration of the oil in the circulating gas is reduced to 0.6% after separation.
Example 4:
an oil separator is arranged at the top of the water scrubber, the structure size is phi 4000 multiplied by 7400, the total gas volume before the circulating gas enters the decarburization unit is 16700Kmol/h, the main components are an oxidation tower, hydrogen, hydrocarbons, carbon dioxide and water, the concentration of the oil is about 8%, the operation pressure is 1.8Mpa, the gas temperature is 40 ℃, the circulating gas enters the separator for separation, and the concentration of the oil in the circulating gas is reduced to 0.5% after separation.
Example 5:
an oil separator is arranged at the top of the water scrubber, the structure size is phi 4000 multiplied 8000, the total gas volume before the circulating gas enters the decarburization unit is 17300Kmol/h, the main components are an oxidation tower, hydrogen, hydrocarbons, carbon dioxide and water, the concentration of the oil is about 7%, the operation pressure is 2.62Mpa, the gas temperature is 42 ℃, the circulating gas enters the separator for separation, and the concentration of the oil in the circulating gas is reduced to 0.7% after separation.
Example 6:
an oil separator is arranged at the top of the water scrubber, the structure size is phi 8000 multiplied by 12000, the total gas quantity before the circulating gas enters the decarburization unit is 44800Kmol/h, the main components are an oxidation tower, hydrogen, hydrocarbons, carbon dioxide and water, the concentration of the oil is about 9 percent, the operation pressure is 3.5Mpa, the gas temperature is 80 ℃, the circulating gas enters the separator for separation, and the concentration of the oil in the circulating gas is reduced to 0.8 percent after separation.
Example 7:
an oil separator is arranged at the top of the water scrubber, the structural size is phi 1600 multiplied by 3500, the total gas volume before the circulating gas enters the decarburization unit is 800Kmol/h, the main components are an oxidation tower, hydrogen, hydrocarbons, carbon dioxide and water, wherein the concentration of the oil is about 8%, the operating pressure is 3.4Mpa, the gas temperature is 40 ℃, the circulating gas enters the separator for separation, and the concentration of the oil in the circulating gas is reduced to 0.5% after separation.
Although the present invention has been described with reference to the preferred embodiments, it should be understood that various changes and modifications can be made therein by those skilled in the art without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (7)
1. A method for recycling oil products by a coal-to-liquid circulating gas decarburization unit is characterized in that the coal-to-liquid circulating gas decarburization unit enables circulating gas from a compressor to enter a purified gas system after passing through a water washing tower and an absorption tower; the method is characterized in that: the circulating gas from the compressor is subjected to oil-gas separation by a separator and then enters a coal-to-liquid circulating gas decarburization unit; leading the circulating gas passing through the separator to a coal-to-liquid circulating gas decarburization unit; the oil product passing through the separator is led to an oil synthesis unit for recovery.
2. The method for recycling the oil product by the coal-to-liquid circulating gas decarburization unit according to claim 1, which is characterized in that: the oil passing through the separator is pumped out by an oil pump.
3. The method for recycling the oil product by the coal-to-liquid circulating gas decarburization unit according to claim 1, which is characterized in that: the oil product is recovered after passing through the condensing unit.
4. The method for recycling the oil product by the coal-to-liquid circulating gas decarburization unit according to claim 1, which is characterized in that: the temperature in the separator is controlled within the range of 30-110 ℃.
5. The method for recycling the oil product by the coal-to-liquid circulating gas decarburization unit according to claim 1, which is characterized in that: the operating pressure in the separator is 0.1-5 MPa.
6. The method for recycling the oil product by the coal-to-liquid circulating gas decarburization unit as claimed in claim 2, wherein: the oil product pump is started to pump oil products when the liquid level in the separator reaches a preset height.
7. The method for recycling the oil product by the coal-to-liquid circulating gas decarburization unit as claimed in claim 2, wherein: the circulating gas from the compressor firstly enters the separator after passing through the on-line analysis equipment, and the oil pump is closed when the oil concentration is less than 90%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011163751.7A CN112592727A (en) | 2020-10-27 | 2020-10-27 | Method for recovering oil product by coal-to-liquid circulating gas decarburization unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011163751.7A CN112592727A (en) | 2020-10-27 | 2020-10-27 | Method for recovering oil product by coal-to-liquid circulating gas decarburization unit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112592727A true CN112592727A (en) | 2021-04-02 |
Family
ID=75180651
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011163751.7A Pending CN112592727A (en) | 2020-10-27 | 2020-10-27 | Method for recovering oil product by coal-to-liquid circulating gas decarburization unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112592727A (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101210186A (en) * | 2006-12-26 | 2008-07-02 | 南化集团研究院 | Solvent and method for removing carbon dioxide from Fischer-Tropsch synthesis circulation gas |
| CN108384572A (en) * | 2018-03-12 | 2018-08-10 | 国家能源投资集团有限责任公司 | A kind of the hydrogen-carbon ratio adjusting method and system of F- T synthesis gas co-producing hydrogen |
-
2020
- 2020-10-27 CN CN202011163751.7A patent/CN112592727A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101210186A (en) * | 2006-12-26 | 2008-07-02 | 南化集团研究院 | Solvent and method for removing carbon dioxide from Fischer-Tropsch synthesis circulation gas |
| CN108384572A (en) * | 2018-03-12 | 2018-08-10 | 国家能源投资集团有限责任公司 | A kind of the hydrogen-carbon ratio adjusting method and system of F- T synthesis gas co-producing hydrogen |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100484894C (en) | Method for treating coal gasification wastewater by single-tower pressurization stripping and device therefor | |
| CN110203986B (en) | System and method for reducing ammonia nitrogen content | |
| CN211545945U (en) | Device for preparing carbon monoxide and hydrogen by cracking methanol | |
| CN105693452A (en) | Purifying system and method for acetylene preparation from natural gas | |
| EP0270040A2 (en) | Process for removing carbon dioxide from a gas | |
| CN106433832A (en) | Process and device for removing CO2 in natural gas | |
| KR101111006B1 (en) | Method and apparatus for recovering hydrogen from petroleum desulfurization | |
| CN101862576B (en) | The method and apparatus of purifying gas mixture by means of physical gas washing | |
| US2891633A (en) | Acetylene separation system | |
| CN104307341A (en) | Flare gas compression and desulphurization technology | |
| CN208166931U (en) | The reprocessing system of F- T synthesis diesel oil distillate | |
| CN103525466A (en) | Method and device for indirectly liquefying coal and separating carbon dioxide | |
| CN112592727A (en) | Method for recovering oil product by coal-to-liquid circulating gas decarburization unit | |
| CN102010733B (en) | Method and device for condensing and recovering shale oil in collecting tube section of oil shale retorting system | |
| CN109355087B (en) | Step recovery device and method for oil product in gas containing oil dust | |
| CN113368663B (en) | Treatment method of Fischer-Tropsch synthesis decarbonized tail gas and equipment system for implementing method | |
| CN202208705U (en) | Device for preparing synthesis gas or hydrogen through BGL pressurizing molten slag gasification with pure oxygen non-catalytic partial oxidation | |
| CN1473911A (en) | Organic sulfur removing and deoxygenation process for producing high pruity CO gas | |
| CN108057319B (en) | Raw material gas recovery method and device | |
| CN104611005A (en) | Process method for increasing coking diesel fuel yield | |
| CN112604456A (en) | Method for removing organic matters in decarburization unit of coal-to-liquid device | |
| CN112850829A (en) | Slag water treatment system | |
| CN106365372A (en) | Solid-particle-containing acidic black water treatment method | |
| CN103789011B (en) | A kind of wax hydrofining post-treating method | |
| CN112811402A (en) | Integrated helium extraction device adopting hydrate method |
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 | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210402 |