CN111957166A - High condensation point waste gas recovery device and recovery method - Google Patents
High condensation point waste gas recovery device and recovery method Download PDFInfo
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- CN111957166A CN111957166A CN202010960688.3A CN202010960688A CN111957166A CN 111957166 A CN111957166 A CN 111957166A CN 202010960688 A CN202010960688 A CN 202010960688A CN 111957166 A CN111957166 A CN 111957166A
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- 239000002912 waste gas Substances 0.000 title claims abstract description 60
- 238000009833 condensation Methods 0.000 title claims abstract description 46
- 230000005494 condensation Effects 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000011084 recovery Methods 0.000 title claims abstract description 20
- 238000002485 combustion reaction Methods 0.000 claims abstract description 20
- 238000005406 washing Methods 0.000 claims abstract description 17
- 239000003513 alkali Substances 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 40
- 239000007788 liquid Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims description 5
- 238000004321 preservation Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000002253 acid Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 abstract description 6
- 238000010521 absorption reaction Methods 0.000 abstract description 5
- 238000001816 cooling Methods 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 52
- 230000000694 effects Effects 0.000 description 7
- 239000010426 asphalt Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- UJOBWOGCFQCDNV-UHFFFAOYSA-N 9H-carbazole Chemical compound C1=CC=C2C3=CC=CC=C3NC2=C1 UJOBWOGCFQCDNV-UHFFFAOYSA-N 0.000 description 2
- TXCDCPKCNAJMEE-UHFFFAOYSA-N dibenzofuran Chemical compound C1=CC=C2C3=CC=CC=C3OC2=C1 TXCDCPKCNAJMEE-UHFFFAOYSA-N 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- RDOWQLZANAYVLL-UHFFFAOYSA-N phenanthridine Chemical compound C1=CC=C2C3=CC=CC=C3C=NC2=C1 RDOWQLZANAYVLL-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- DXBHBZVCASKNBY-UHFFFAOYSA-N 1,2-Benz(a)anthracene Chemical compound C1=CC=C2C3=CC4=CC=CC=C4C=C3C=CC2=C1 DXBHBZVCASKNBY-UHFFFAOYSA-N 0.000 description 1
- FMMWHPNWAFZXNH-UHFFFAOYSA-N Benz[a]pyrene Chemical compound C1=C2C3=CC=CC=C3C=C(C=C3)C2=C2C3=CC=CC2=C1 FMMWHPNWAFZXNH-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- -1 carbocyclic hydrocarbon Chemical class 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B1/00—Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser
- F28B1/02—Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser using water or other liquid as the cooling medium
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B9/00—Auxiliary systems, arrangements, or devices
- F28B9/08—Auxiliary systems, arrangements, or devices for collecting and removing condensate
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
Abstract
A high condensation point waste gas recovery device is characterized by comprising a heat exchanger, a waste oil tank, an alkaline washing tower and a fan, wherein a waste gas inlet pipe is arranged at the top end of the heat exchanger, and a discharge pipe is arranged at the bottom end of the heat exchanger; the feeding end of the dirty oil tank is connected with the discharging end of the discharging pipe, and the top end of the dirty oil tank is provided with a waste gas outlet; the middle part or the bottom of the alkaline tower is provided with a waste gas inlet, the top of the alkaline tower is provided with an exhaust port, the upper part of the alkaline tower is provided with an alkaline liquor inlet, and the lower part of the alkaline tower is provided with an alkaline liquor outlet; and the air inlet end of the combustion equipment is connected with the exhaust port of the alkaline washing tower. The invention also discloses a method for recovering the waste gas with the high condensation point. The treatment of cooling, alkali liquor absorption and combustion is adopted, C5 and C5+ components are finally condensed and collected in a sump oil tank, and C4 and the following light components are sent to combustion equipment to complete combustion.
Description
Technical Field
The invention relates to a waste gas treatment device, in particular to a recovery device for waste gas with a high condensation point. The invention also relates to a method for recovering the high condensation point waste gas.
Background
Since the 80 s in the 20 th century, China began to organically conduct development and research and technical introduction in the aspect of oil and gas recovery, and certain achievements were achieved. However, most of the oil gas treatment processes and treatment facilities aim at the light oil gas treatment, and with the stricter environmental requirements, the crude oil inlet amount is increased, and the treatment and recovery of the waste gas with a high condensation point are also paid more and more attention.
It is known that the oil and gas components of exhaust gas with high condensation point such as asphalt are complex and include carbocyclic hydrocarbon, cyclic hydrocarbon derivatives and other compounds, such as benzopyrene, benzanthracene, carbazole, dibenzofuran, phenanthridine, etc. At the present stage, because heavy oil and gas components are complex and the recovery economic benefit is limited, domestic refining generally adopts a mode of directly communicating air through a vent hole to directly discharge oil and gas to the atmosphere, which is not in accordance with the large direction of creating a green and environment-friendly chemical production mode in China, and therefore treatment is required before the atmosphere is discharged.
The currently common oil and gas treatment modes mainly comprise the following or a combination thereof: 1. condensation method. 2. Absorption method. 3. Adsorption method. 4. A membrane separation method. 5. A combustion method.
In the traditional treatment mode of condensation and absorption, the high condensation point waste gas needs to be cooled to-130 ℃ so as to completely condense C2 and above components in the high condensation point waste gas. The method has high cost, and aims at the waste gas with high condensation point, and the risk of blocking the condenser after the recombination and the condensation in the oil gas exist in the condensation process.
The membrane separation method can cause the condition that the cementing oil in oil gas is attached to a separation membrane to influence the separation effect when the membrane separation method is used in the process of high condensation point waste gas.
The method for directly adsorbing the waste gas with the high condensation point can lead the adsorbent in the adsorption tank to be quickly saturated and difficult to desorb due to the colloidal condensate in the condensate.
Disclosure of Invention
The first technical problem to be solved by the present invention is to provide a high condensation point exhaust gas recovery device with low cost and environmental protection requirement after exhaust gas treatment, aiming at the above technical situation.
The second technical problem to be solved by the present invention is to provide a method for recovering waste gas with high condensation point, which has low cost and meets the environmental protection requirement after waste gas treatment, in view of the above technical situation.
The technical scheme adopted by the invention for solving the first technical problem is as follows: a high condensation point waste gas recovery device is characterized by comprising
The heat exchanger is provided with a waste gas inlet pipe at the top end and a discharge pipe at the bottom end, and is provided with a first pipe layer capable of containing cooling water;
the feeding end of the dirty oil tank is connected with the discharging end of the discharging pipe, and the top end of the dirty oil tank is provided with a waste gas outlet;
the middle part or the bottom of the alkaline washing tower is provided with a waste gas inlet, the top of the alkaline washing tower is provided with an exhaust port, the upper part of the alkaline washing tower is provided with an alkaline liquor inlet, and the lower part of the alkaline washing tower is provided with an alkaline liquor outlet;
the fan is used for conveying the waste gas from the sump oil tank to the alkaline washing tower; and
and the air inlet end of the combustion equipment is connected with the exhaust port of the alkaline washing tower.
The periphery of the waste gas inlet pipe is sleeved with a steam tracing pipe and a heat insulation layer. The steam heat tracing pipe periphery is located to the heat preservation, and the steam heat tracing pipe can ensure that the waste gas intake pipe maintains certain temperature, can effectively avoid among the oil gas transportation process heavy ends to condense in the pipeline.
Furthermore, a liquid level sensor is arranged in the dirty oil tank, and a valve linked with the liquid level sensor is arranged on the waste gas inlet pipe.
Furthermore, the first pipe layer is also connected with a first steam inlet pipe and a first condensed water outlet pipe. Because high condensation point waste gas component is complicated, like pitch etc. can appear that colloidal sump oil adheres to in cooler shell inner wall and tube layer outer wall, influences the heat transfer effect. And the heat exchange effect is judged by monitoring the temperature at the outlet of the heat exchanger. When the heat transfer effect descends obviously, the circulating cooling water of the first pipe layer and the jacket layer is discharged, steam is introduced, and the attached colloidal dirty oil is liquefied and collected to the dirty oil tank through heating.
The dirty oil tank have the second pipe layer, this second pipe layer is connected with second steam intake pipe and second condensate outlet pipe. And the bottom of the sump oil tank is connected with a condensate output pipe. Steam is introduced into the pipe layer or the jacket for heating, the temperature of the condensed oil is increased, the fluidity of the condensed oil is increased, and the condensed oil is conveyed to a refinery sump oil tank area for recycling through a sump oil pump and a condensate output pipe.
The technical scheme adopted by the invention for solving the second technical problem is as follows: a recovery method using a high condensation point waste gas recovery device is characterized by comprising the following steps:
the high condensation point waste gas is subjected to heat preservation and tracing and is kept at 130 ℃, the high condensation point waste gas enters a first shell of a heat exchanger from a waste gas inlet pipe, the heat exchanger cools the high condensation point waste gas in the first shell to 35 ℃, and C5 and C5+ components in oil gas are condensed and collected in a sump oil tank; the high condensation point waste gas without heavy components enters an alkaline tower through a fan, acid components in oil gas are removed through alkali liquor, the treated oil gas mainly contains C4 and below light components and is sent to combustion equipment, and the oil gas is finally discharged after combustion.
Compared with the prior art, the invention has the advantages that: the treatment of cooling, alkali liquor absorption and combustion is adopted, C5 and C5+ components are finally condensed and collected in a sump oil tank, and C4 and the following light components are sent to combustion equipment to complete combustion.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1, the high condensation point exhaust gas recovery apparatus in the present embodiment includes a heat exchanger 1, a waste oil tank 2, an alkaline tower 3, a fan 6, and a combustion device 4.
The top end of the heat exchanger 1 is provided with a waste gas inlet pipe 5, the bottom end of the heat exchanger is provided with a discharge pipe 14, and the heat exchanger is provided with a first pipe layer 12 capable of containing cooling water; the periphery of the exhaust gas inlet pipe 5 in this embodiment is sleeved with a steam heat tracing pipe 51 and a heat insulating layer, and the heat insulating layer is located at the periphery of the steam heat tracing pipe 51 (not shown in the figure). The steam heat tracing pipe 51 can ensure that the exhaust gas inlet pipe 5 maintains a constant temperature of 130 ℃, and can effectively avoid heavy components from condensing in the pipeline in the oil gas conveying process. The first pipe layer 12 in this embodiment is connected with a circulating water inlet pipe 17 and a circulating water outlet pipe 18.
The heat exchanger 1 also has a jacket layer 13. A first steam inlet pipe 15 and a first condensate outlet pipe 16 are also connected to the first pipe layer 12. Because high condensation point waste gas component is complicated, like pitch etc. can appear that colloidal sump oil adheres to in cooler shell inner wall and tube layer outer wall, influences the heat transfer effect. And the heat exchange effect is judged by monitoring the temperature at the outlet of the heat exchanger. When the heat transfer effect descends obviously, the circulating cooling water of the first pipe layer and the jacket layer is discharged, steam is introduced, and the attached colloidal dirty oil is liquefied and collected to the dirty oil tank through heating.
The feeding end of the dirty oil tank 2 is connected with the discharging end of the discharging pipe 14, and the top end of the dirty oil tank 2 is provided with a waste gas outlet; a liquid level sensor 22 is arranged in the dirty oil tank 2, and a valve 23 linked with the liquid level sensor 22 is arranged on the waste gas inlet pipe 5. As the level of the collected condensate rises to a set value, the valve 23 is automatically closed in an interlocked manner, so that the discharge pipe 14 is closed.
The dirty-oil tank 2 has a second pipe layer 21, and a second steam inlet pipe 211 and a second condensed water outlet pipe 212 are connected to the second pipe layer 21. The bottom of the slop oil tank 2 is connected with a condensate output pipe 22. Let in steam heating in the second pipe layer 21, improve the condensate temperature, increase the mobility of condensate, export the condensate outward through sump oil pump and condensate output pipe and be used for the remill to refinery sump oil jar district. Of course, the dirty oil tank 2 in this embodiment may have a jacket layer through which steam is introduced.
The middle lower part of the alkaline tower 3 is provided with a waste gas inlet, the top is provided with an exhaust port, the upper part is provided with an alkali liquor inlet, the lower part is provided with an alkali liquor outlet, the alkali liquor inlet is connected with a liquid inlet pipe 31, and the alkali liquor outlet is connected with a liquid outlet pipe 32. The fan 6 is used for conveying the waste gas from the sump oil tank 2 to the alkaline washing tower 3; the air inlet end of the combustion device 4 is connected with the air outlet of the alkaline washing tower 3, and the gas combusted by the combustion device 4 is discharged into the atmosphere.
The recovery method comprises the following steps:
the high condensation point waste gas is subjected to heat preservation and tracing and is kept at 130 ℃, the high condensation point waste gas enters a first shell of the heat exchanger 1 from the waste gas inlet pipe 5, the heat exchanger 1 cools the high condensation point waste gas in the first shell to 35 ℃, and C5 and C5+ components in oil gas are condensed and collected in the sump oil tank 2; the high condensation point waste gas from which heavy components are removed enters an alkaline tower 3 through a fan 6, acid components in oil gas are removed through alkali liquor, the treated oil gas mainly contains C4 and light components below, the light components are sent to a combustion device 4, and the light components are finally discharged after combustion.
This embodiment carries out high condensation point exhaust-gas treatment, can effectively avoid the direct exhaust condition of tank field oil gas. Aiming at the conditions that the tail gas of the asphalt has heavy smell and heavy components and paraffin components are more and easy to condense, the pretreatment mode of water-cooled desulphurization has the advantages of low cost, short flow, stable operation and the like. The water cooling unit adopts a jacket heat exchanger and a sump oil tank with a coil to be heated, and can effectively treat asphalt wax condensed and attached to the surface of equipment. The subsequent desulfurization unit can effectively remove H of the asphalt oil gas2And the S component eliminates the peculiar smell of tail gas. Finally, the mixture enters combustion equipment, and is fully oxidized and discharged after reaching the national environmental protection discharge standard.
The embodiment aims at the process characteristics of the waste gas with high condensation point such as asphalt, liquid sulfur and the like, combines the combined mode of cooling, alkali washing absorption and combustion for treatment, and purposefully sets equipment to treat each component in the oil gas in a layered mode, thereby finally achieving the purpose of qualified emission. The method has the advantages of low investment, short flow, stable operation and the like, and has strong feasibility in the aspect of domestic high condensation point waste gas treatment.
Claims (7)
1. A high condensation point waste gas recovery device is characterized by comprising
The heat exchanger (1) is provided with a waste gas inlet pipe (5) at the top end, a discharge pipe (14) at the bottom end and a first pipe layer (12) capable of containing cooling water;
the feed end of the dirty oil tank (2) is connected with the discharge end of the discharge pipe (14), and the top end of the dirty oil tank (2) is provided with a waste gas outlet;
the middle part or the bottom of the alkaline washing tower (3) is provided with a waste gas inlet, the top of the alkaline washing tower is provided with an exhaust port, the upper part of the alkaline washing tower is provided with an alkaline liquor inlet, and the lower part of the alkaline washing tower is provided with an alkaline liquor outlet;
the fan (6) is used for conveying the waste gas from the sump oil tank (2) to the alkaline washing tower (3); and
and the air inlet end of the combustion equipment (4) is connected with the exhaust port of the alkaline washing tower (3).
2. The waste gas recovery device with high condensation point according to claim 1, characterized in that the waste gas inlet pipe (5) is sleeved with a steam heat tracing pipe (51) and an insulating layer.
3. The high condensation point waste gas recovery device according to claim 1, characterized in that a liquid level sensor (22) is arranged in the sump oil tank (2), and a valve (23) linked with the liquid level sensor (22) is arranged on the waste gas inlet pipe (5).
4. The exhaust gas recovery device with high condensation point according to claim 1, characterized in that a first steam inlet pipe (15) and a first condensed water outlet pipe (16) are further connected to the first pipe layer (12).
5. The apparatus for recycling exhaust gas with high condensation point according to claim 1, characterized in that the sump oil tank (2) has a second pipe layer (21), and a second steam inlet pipe (211) and a second condensed water outlet pipe (212) are connected to the second pipe layer (21).
6. The exhaust gas recovery device with high condensation point according to claim 1, characterized in that a condensate outlet pipe (22) is connected to the bottom of the slop oil tank (2).
7. A recycling method using the high condensation point exhaust gas recycling device according to claim 2, characterized by comprising the steps of:
the high condensation point waste gas is subjected to heat preservation and tracing and is kept at 130 ℃, the high condensation point waste gas enters a first shell of the heat exchanger (1) from the waste gas inlet pipe (5), the heat exchanger (1) cools the high condensation point waste gas in the first shell to 35 ℃, and C5 and C5+ components in oil gas are condensed and collected in the sump oil tank (2); the high condensation point waste gas from which heavy components are removed enters an alkaline tower (3) through a fan (6), acid components in oil gas are removed through alkali liquor, the treated oil gas mainly contains C4 and light components below, then the treated oil gas is sent to a combustion device (4), and finally the treated oil gas is discharged after combustion.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113842678A (en) * | 2021-09-30 | 2021-12-28 | 中化蓝天霍尼韦尔新材料有限公司 | Separation system and method for non-condensable gas in refrigerant |
| CN114225617A (en) * | 2021-12-17 | 2022-03-25 | 镇海石化工程股份有限公司 | Method for treating heavy oil gas with high condensation point |
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