CN111420519B - System and method for treating oil gas - Google Patents
System and method for treating oil gas Download PDFInfo
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- CN111420519B CN111420519B CN202010275673.3A CN202010275673A CN111420519B CN 111420519 B CN111420519 B CN 111420519B CN 202010275673 A CN202010275673 A CN 202010275673A CN 111420519 B CN111420519 B CN 111420519B
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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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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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
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
Abstract
A system and method for processing oil gas, the system includes an absorption tower, a buffer tank, two adsorption towers; the absorption tower is connected with the buffer tank, and the buffer tank and the two adsorption towers are connected in series; the two adsorption towers are connected in series or in parallel. Oil gas is firstly subjected to absorption-buffering-adsorption flow, and most organic matters are removed in an absorption tower; the standard discharge is realized after the adsorption tower; when the absorption tower is close to saturation, cutting out the system for desorption operation; the operation mode of buffering, adsorption and adsorption is changed, wherein a buffer tank is connected with two adsorption towers in series; most of organic matters are removed in the first adsorption tower, and the standard emission is realized after the second adsorption tower; when the absorption tower finishes desorption and the first absorption tower is close to saturation, the absorption-buffering-absorption operation of the absorption tower, the buffer tank and the second absorption tower is changed, the first absorption tower is cut off for regeneration, and continuous operation can be realized. The invention prolongs the service cycle of the adsorbent and reduces the energy consumption; and is suitable for occasions with large changes of oil gas content and flow.
Description
Technical Field
The invention belongs to the technical field of chemical industry and environmental protection, and particularly relates to a system and a method for treating volatile oil gas.
Background
In the oil storage, loading and unloading processes in the chemical production process, a large amount of Volatile Organic Compounds (VOCs) are often generated, and the oil storage, loading and unloading processes have the actual current situations of strong dispersity, multiple components, large molecular weight difference, large physical property difference and the like. Methods for treating volatile organic compound-containing gases generally include condensation, oxidation, absorption, adsorption, and the like. The condensation method has strict requirements on the content of oil gas, and the lower the content of the oil gas is, the higher the condensation energy consumption is. The oxidation method has strict requirements on the content of oil and gas (considering the explosion limit) and has the defect of high energy consumption (when the content of the oil and gas is low, external fuel is needed). Therefore, it is very important to enrich the oil gas by using an absorption method and an adsorption method. But the absorption method has wide applicability and limited removal rate, and is difficult to directly reach the discharge standard. Various porous materials (such as activated carbon and silica gel) are commonly used in the adsorption method, and the adsorption method has the advantages of simple and safe process and high removal efficiency. However, the activated carbon material commonly used in the adsorption method has many micropores and poor recycling performance. Recently, mesoporous materials such as carbon nanotubes and graphene have been developed rapidly, and long-period recycling of adsorption and desorption can be realized, so that the mesoporous material is the most promising technology.
However, the oil gas generated in the oil storage and loading and unloading process has unstable flow and large impact on the adsorbent. Not only can cause unqualified treatment, but also has the defect of increasing energy consumption due to frequent regeneration of the adsorbent.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a system and a method for treating oil gas, which adopt the matching use of an absorption method and an adsorption method to treat volatile organic compounds, so as to solve the problem that the desorbed gaseous organic compounds are difficult to treat, increase the treatment measures for the volatile organic compounds with large flow fluctuation or concentration fluctuation, reduce the energy consumption and improve the added value of products.
In order to achieve the purpose, the invention adopts the following technical scheme:
a system for treating oil gas comprises an absorption tower 1, a buffer tank 2, two absorption towers, namely a first absorption tower 3 and a second absorption tower 4, wherein the middle part of the absorption tower 1 is provided with a gas inlet 5 containing volatile organic compounds and a liquid absorbent feeding port 6, and the top part of the absorption tower is provided with an absorption tower gas outlet 7; the top of the buffer tank 2 is provided with an absorbed gas inlet 8 and a deoiled gas outlet 9 which are communicated with the gas outlet 7 of the absorption tower, the absorbed gas inlet 8 is also communicated with an inlet pipeline for directly absorbing fresh oil gas, the inlet pipeline is provided with a fourth valve d, and the bottom of the buffer tank 2 is provided with a condensate outlet 10; the bottom of the first adsorption tower 3 is provided with a first adsorption tower gas inlet 11 communicated with the deoiled gas outlet 9, and the top of the first adsorption tower is provided with a first adsorption tower adsorbed gas outlet 12; the bottom of the second adsorption tower 4 is provided with a second adsorption tower gas inlet 13 communicated with the first adsorption tower adsorbed gas outlet 12, and the top of the second adsorption tower 4 is provided with a second adsorption tower adsorbed gas outlet 14; the absorption tower 1 is connected with the buffer tank 2 in series, the buffer tank 2 is connected with the first absorption tower 3 and the second absorption tower 4 in series, and the first absorption tower 3 is connected with the second absorption tower 4 in series or in parallel.
The absorption tower 1 is filled with liquid hydrocarbon absorbent, the boiling point of which is 200-300 ℃, and the freezing point of which is minus 10 ℃ to minus 50 ℃.
The gas inlet of the absorption tower 1 containing volatile organic compounds enters from the middle of the absorption tower 1 and extends to the bottom, so that the oil gas entering the absorption tower 1 has sufficient contact time with the liquid hydrocarbon absorbent.
A baffle plate is arranged in the middle of the buffer tank 2, so that the gas entering from the gas inlet 8 after absorption has enough residence time in the buffer tank; the operating temperature of the buffer tank 2 is minus 30 ℃ to 10 ℃.
The baffle plate in the middle of the buffer tank 2 is a vertical baffle plate.
The first adsorption tower 3 and the second adsorption tower 4 are filled with easily-regenerated adsorbents, and the easily-regenerated adsorbents contain one or more materials of acid clay, alumina, molecular sieves, activated carbon fibers, carbon nanotubes and graphene.
The method for treating oil and gas by the system comprises the following steps:
a) sequentially connecting an absorption tower 1, a buffer tank 2, a first adsorption tower 3 and a second adsorption tower 4;
b) adding a liquid hydrocarbon absorbent into the absorption tower 1 from a liquid absorbent feeding port 6, and respectively feeding the absorbent into the first absorption tower 3 and the second absorption tower 4;
c) firstly, an absorption tower 1, a buffer tank 2 and a first absorption tower 3) are adopted for series operation; introducing gas containing volatile organic compounds from a first valve a of a gas inlet 5 containing the volatile organic compounds of an absorption tower 1, after the gas is absorbed by a liquid hydrocarbon absorbent, most of oil gas is changed into liquid and is left in a liquid phase, a small amount of oil gas is introduced into a buffer tank 2 from a third valve c of a gas outlet 7 of the absorption tower along with the gas through a gas inlet 8 after the absorption, a small amount of oil in the gas is condensed, and the gas is periodically discharged from a fifth valve e of a condensate outlet 10;
d) gas is discharged from the buffer tank 2 from the deoiled gas outlet 9, enters the first adsorption tower 3 through the first adsorption tower gas inlet 11, passes through an adsorbent layer of the first adsorption tower 3, is adsorbed on the adsorbent, and is discharged from a seventh valve g of a gas outlet 12 after being adsorbed by the first adsorption tower at the top of the first adsorption tower 3, and is discharged after reaching the standard;
e) when the liquid hydrocarbon absorbent of the absorption tower 1 is close to saturation, closing a first valve a of a gas inlet 5 containing volatile organic compounds of the absorption tower 1, a second valve b of a gas outlet 7 of the absorption tower and a third valve c, cutting the absorption tower 1 out, and desorbing for later use; changing the operation mode to the series operation among the buffer tank 2, the first adsorption tower 3 and the second adsorption tower 4; the unabsorbed oil gas is directly introduced into the buffer tank 2 through the fourth valve d and the absorbed gas inlet 8, is discharged from the deoiled gas outlet 9, enters the first adsorption tower 3 through the gas inlet 11 of the first adsorption tower, and the oil gas discharged from the eighth valve h of the gas outlet 12 absorbed by the first adsorption tower enters the second adsorption tower 4 through the gas inlet 13 of the second adsorption tower for adsorption operation, and then the gas is discharged from the gas outlet 14 absorbed by the second adsorption tower and is discharged after reaching the standard;
f) when the first adsorption tower 3 is close to saturation, closing a ninth valve i of a gas inlet 11 of the first adsorption tower and a seventh valve g and an eighth valve h of a gas outlet 12 of the first adsorption tower after adsorption; cutting out the first adsorption tower 3, and performing desorption operation for later use; the series operation of the absorption tower 1, the buffer tank 2 and the second adsorption tower 4 is changed, namely, after the gas is deoiled, a gas outlet 9 is discharged from the buffer tank 2 and enters the second adsorption tower 4 through a sixth valve f and a second adsorption tower gas inlet 13, after passing through an adsorbent layer of the second adsorption tower 4, organic matters are adsorbed on the adsorbent, and the adsorbed gas is discharged from a second adsorption tower at the top of the second adsorption tower 4 through a gas outlet 14 after being adsorbed, and reaches the standard and is discharged;
g) when the second adsorption tower 4 is close to saturation, the second adsorption tower 4 is cut out, and the desorption operation is carried out for standby; the operation mode is changed to: the absorption tower 1, the buffer tank 2 and the first absorption tower 3 are operated in series, and the steps c-g are repeated.
When the absorption tower 1 executes the absorption operation, the temperature is 30-10 ℃ below zero, the absolute pressure is 120-500kPa, and the absorption rate is 75-95%.
When the first adsorption tower 3 or the second adsorption tower 4 executes the adsorption operation, the temperature is 30-10 ℃ below zero, and the absolute pressure is 100-; the adsorption effect is as follows: the content of non-methane total hydrocarbon in the inert gas is less than 50ppm, and the content of aromatic hydrocarbon compound is less than 4 ppm.
The main body of the gas containing volatile organic compounds is inert gas (nitrogen, argon, CO)2Etc.) wherein the volume concentration of the volatile organic compounds is 0.01-2%, and the components are organic compounds with the molecular weight of 26-150.
Compared with the prior art, the invention has the beneficial effects that:
(1) compared with the traditional absorption-desorption technology, the invention adopts two ways of absorption and adsorption, breaks the liquid-liquid balance in the absorption process and has the advantage of high absorption rate.
(2) Compared with the single adsorption-desorption technology, the invention can effectively reduce the impact on the adsorbent because most organic matters are removed by the absorption operation. The service cycle of the following adsorbent is prolonged by 50-180%, the desorption frequency is reduced by more than 50%, and the comprehensive energy consumption is reduced by 40-50%.
(3) Compared with the technology of double absorption and double adsorption, the invention saves one absorption tower and reduces the cost by 20 percent.
(4) Compared with the technology of filling the activated carbon adsorbent, the adsorbent of the invention has the advantages of long service cycle of 90-99%, reduced regeneration energy consumption of 50% and shortened regeneration time of 50%.
(5) The arrangement of the buffer tank with the baffle plate and the low-temperature operation effectively prevent the liquid hydrocarbon absorbent from polluting the subsequent absorbent, and prolong the service life of the absorbent by 50-100 percent.
Drawings
FIG. 1 is a block diagram of the system of the present invention.
Wherein, 1, the absorption tower (gas feed pipe enters from the middle and is inserted into the bottom); 2. the adsorption tower comprises a buffer tank (a vertical baffle plate is arranged inside the buffer tank), 3, a first adsorption tower, 4, a second adsorption tower, 5, a gas inlet containing volatile organic compounds, 6, a liquid absorbent adding inlet, 7, an absorption tower gas outlet, 8, an absorbed gas inlet, 9, a deoiled gas outlet, 10, a condensate outlet, 11, a first adsorption tower gas inlet, 12, a first adsorption tower absorbed gas outlet, 13, a second adsorption tower gas inlet and 14, a second adsorption tower absorbed gas outlet.
a. The valve comprises a first valve, a second valve, a third valve, a fourth valve, a fifth valve, a sixth valve, a seventh valve, an eighth valve and a ninth valve.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
Example 1
As shown in fig. 1, an absorption tower (1), a buffer tank (2), a first adsorption tower (3) and a second adsorption tower (4) are connected in sequence; liquid hydrocarbon absorbent (boiling point of 200-250 ℃, freezing point of-50 to-30 ℃) is added into the absorption tower (1) from a liquid absorbent adding port (6). Filling adsorbents (30% of activated carbon and 70% of graphene in mass fraction) into a first adsorption tower (3); and (3) filling an adsorbent (90% of carbon nano tubes and 10% of graphene in mass fraction) into the second adsorption tower (4).
Firstly, an absorption tower (1), a buffer tank (2) and a first absorption tower (3) are adopted to carry out series operation. Oil gas (the main gas is nitrogen, the volume concentration of volatile organic compounds is 2 percent, and the component is C)4-C10Hydrocarbon) was introduced from the volatile organic compound-containing gas inlet (5) of the absorption column (1), operated at a temperature of-30 ℃ and a pressure of 500kPa (absolute) with an absorption of 90%. After being absorbed by the liquid hydrocarbon absorbent, most of oil gas is changed into liquid and is remained in a liquid phase, a small amount of oil gas is led into the buffer tank (2) from the gas outlet (7) of the absorption tower along with the gas through the gas inlet (8) after absorption, the operation is carried out at the temperature of minus 30 ℃, a small amount of oil in the gas is condensed, and the condensed oil is periodically discharged from the condensed liquid outlet (10).
And secondly, gas is discharged from a buffer tank from a deoiled gas outlet (9), enters a first adsorption tower (3) through a first adsorption tower gas inlet (11), the adsorption temperature is-30 ℃, the pressure is 480kPa (absolute pressure), organic matters are adsorbed on an adsorbent after passing through an adsorbent layer in the first adsorption tower (3), and the treated gas (nitrogen, wherein the non-methane total hydrocarbon is 35ppm, and the aromatic hydrocarbon is 3ppm) is discharged from a first adsorption tower adsorption outlet (12).
And thirdly, when the liquid hydrocarbon absorbent in the absorption tower (1) is close to saturation, closing the gas inlet (5) containing the volatile organic compounds in the absorption tower (1), cutting off the absorption tower (1), and desorbing for later use. The operation mode is changed into a series operation between the buffer tank (2), the first adsorption tower (3) and the second adsorption tower (4). Oil gas (main gas is nitrogen, organic matter is 2%, C)4-C10Hydrocarbon) was passed directly through the post-absorption gas inlet (8) into the surge tank (2) and operated at-30 ℃. And the gas is discharged from the deoiled gas outlet (9) and enters the first adsorption tower (3) through the gas inlet (11) of the first adsorption tower. The adsorption temperature is-30 ℃ and the pressure is 480kPa (absolute pressure), organic matters are adsorbed on the adsorbent after passing through the adsorbent layer in the first adsorption tower (3), oil gas from the gas outlet (12) after adsorption of the organic matters in the first adsorption tower enters the second adsorption tower (4) through the gas inlet (13) of the second adsorption tower for adsorption operation, the adsorption temperature is-20 ℃, the pressure is 460kPa (absolute pressure), and the organic matters are adsorbed after passing through the adsorbent layer in the second adsorption tower (4)On the adsorbent, then, a gas (nitrogen gas, wherein the non-methane total hydrocarbons are 35ppm, the aromatic hydrocarbons are 3ppm) is discharged from the gas outlet (14) after adsorption in the second adsorption column.
And fourthly, closing the gas inlet (11) of the first adsorption tower when the first adsorption tower (3) is close to saturation. The first adsorption tower (3) is cut out and is ready for use after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the second adsorption tower (4). After the second step, the gas is discharged from the buffer tank (2) through a deoiled gas outlet (9), enters the second adsorption tower (4) through a gas inlet (13) of the second adsorption tower, is adsorbed on the adsorbent after passing through an adsorbent layer of the second adsorption tower (4), and then is discharged from a gas (nitrogen, wherein the non-methane total hydrocarbon is 35ppm, and the aromatic hydrocarbon is 3ppm) after being adsorbed by the second adsorption tower through an outlet (14).
And fifthly, when the second adsorption tower (4) is close to saturation, cutting off the second adsorption tower (4) for standby after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the first absorption tower (3), and the steps are repeated.
Example 2
As shown in fig. 1, an absorption tower (1), a buffer tank (2), a first adsorption tower (3) and a second adsorption tower (4) are connected in sequence; liquid hydrocarbon absorbent (boiling point of 200-300 ℃, freezing point of-30-10 ℃) is added into the absorption tower from a liquid absorbent adding port (6). Filling adsorbents (30% of activated carbon and 70% of graphene in mass fraction) into a first adsorption tower (3); and (3) filling an adsorbent (90% of carbon nano tubes and 10% of graphene in mass fraction) into the second adsorption tower (4).
Firstly, an absorption tower (1), a buffer tank (2) and a first absorption tower (3) are adopted to carry out series operation. Oil gas (the main gas is nitrogen, the volume concentration of volatile organic compounds is 0.5 percent, and the component is gasoline hydrocarbon) is introduced from a gas inlet (5) containing the volatile organic compounds in an absorption tower (1), the absorption temperature is 10 ℃, the pressure is 120kPa (absolute pressure), and the absorption rate is 90 percent. After being absorbed by the liquid hydrocarbon absorbent, most of oil gas is changed into liquid and is remained in a liquid phase, a small amount of oil gas is led into the buffer tank (2) from the gas outlet (7) of the absorption tower along with the gas through the gas inlet (8) after absorption, the operation is carried out at the temperature of 10 ℃, a small amount of oil in the gas is condensed, and the condensed oil is periodically discharged from the condensed liquid outlet (10).
Secondly, gas is discharged from a buffer tank from a deoiled gas outlet (9), enters a first adsorption tower (3) through a first adsorption tower gas inlet (11), the adsorption temperature is 10 ℃, the pressure is 100kPa (absolute pressure), organic matters are adsorbed on an adsorbent after passing through an adsorbent layer in the first adsorption tower (3), and the treated gas (nitrogen, wherein the content of non-methane total hydrocarbons is 35ppm, and the content of aromatic hydrocarbons is 3ppm) is discharged from a first adsorption tower after adsorption at an outlet (12) reaching the standard;
and thirdly, when the liquid hydrocarbon absorbent in the absorption tower (1) is close to saturation, closing the gas inlet (5) containing the volatile organic compounds in the absorption tower (1), cutting off the absorption tower (1), and desorbing for later use. The operation mode is changed into a series operation between the buffer tank (2), the first adsorption tower (3) and the second adsorption tower (4). Oil gas (the main gas is nitrogen, and the organic matter is gasoline hydrocarbon of 0.5%) is directly introduced into the buffer tank (2) through the gas inlet (8) after absorption, and the operation is carried out at 10 ℃. And the gas is discharged from the deoiled gas outlet (9) and enters the first adsorption tower (3) through the gas inlet (11) of the first adsorption tower. The adsorption temperature is 10 ℃, the pressure is 120kPa (absolute pressure), organic matters are adsorbed on the adsorbent after passing through an adsorbent layer in the first adsorption tower (3), oil gas from a gas outlet (12) after adsorption in the first adsorption tower enters the second adsorption tower (4) through a gas inlet (13) of the second adsorption tower for adsorption operation, the adsorption temperature is-10 ℃, the pressure is 100kPa (absolute pressure), the organic matters are adsorbed on the adsorbent after passing through the adsorbent layer in the second adsorption tower (4), and treated gas (nitrogen, wherein the non-methane total hydrocarbon content is 40ppm, and the aromatic hydrocarbon content is 4ppm) is discharged from a gas outlet (14) after adsorption in the second adsorption tower and is discharged after reaching the standard.
And fourthly, closing the gas inlet (11) of the first adsorption tower when the first adsorption tower (3) is close to saturation. The first adsorption tower (3) is cut out and is ready for use after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the second adsorption tower (4). After the second step, the gas is discharged from the buffer tank (2) through a deoiled gas outlet (9), enters the second adsorption tower (4) through a gas inlet (13) of the second adsorption tower, passes through an adsorbent layer of the second adsorption tower (4), the organic matters are adsorbed on the adsorbent, and the treated gas (nitrogen, wherein the non-methane total hydrocarbon is 40ppm, and the aromatic hydrocarbon is 4ppm) is discharged from a gas outlet (14) after being adsorbed by the second adsorption tower, and reaches the standard and is discharged.
And fifthly, when the second adsorption tower (4) is close to saturation, cutting off the second adsorption tower (4) for standby after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the first absorption tower (3), and the steps are repeated.
Example 3
As shown in fig. 1, an absorption tower (1), a buffer tank (2), a first adsorption tower (3) and a second adsorption tower (4) are connected in sequence; liquid hydrocarbon absorbent (boiling point of 200-300 ℃, freezing point of-30-10 ℃) is added into the absorption tower from a liquid absorbent adding port (6). Filling an adsorbent (graphene) in a first adsorption tower (3); the second adsorption tower (4) is filled with an adsorbent (carbon nanotube).
Firstly, an absorption tower (1), a buffer tank (2) and a first absorption tower (3) are adopted to carry out series operation. Oil gas (the main gas is nitrogen, the volume concentration of volatile organic compounds is 0.5%, the components are a mixture of pentane, cyclohexene, cyclohexane, cyclohexanol, benzene and cyclohexanone in any proportion) is introduced from a gas inlet (5) containing the volatile organic compounds in an absorption tower (1), the absorption temperature is 0 ℃, the pressure is 400kPa (absolute pressure), and the absorption rate is 80%. After being absorbed by the liquid hydrocarbon absorbent, most of oil gas is changed into liquid and is remained in a liquid phase, a small amount of oil gas is led into the buffer tank (2) from the gas outlet (7) of the absorption tower along with the gas through the gas inlet (8) after absorption, the operation is carried out at the temperature of minus 10 ℃, a small amount of oil in the gas is condensed, and the condensed oil is periodically discharged from the condensed liquid outlet (10).
Secondly, gas is discharged from a buffer tank from a deoiled gas outlet (9), enters a first adsorption tower (3) through a first adsorption tower gas inlet (11), the adsorption temperature is-10 ℃, the pressure is 380kPa (absolute pressure), organic matters are adsorbed on an adsorbent after passing through an adsorbent layer in the first adsorption tower (3), and the treated gas (nitrogen, wherein the non-methane total hydrocarbon is 35ppm, and the aromatic hydrocarbon is 3ppm) is discharged from a first adsorption tower adsorption outlet (12);
third step, when absorbingWhen the liquid hydrocarbon absorbent in the tower (1) is nearly saturated, the gas inlet (5) of the absorption tower (1) containing volatile organic compounds is closed, the absorption tower (1) is cut off, and the liquid hydrocarbon absorbent is desorbed for use. The operation mode is changed into a series operation between the buffer tank (2), the first adsorption tower (3) and the second adsorption tower (4). Oil gas (the main gas is nitrogen, the volume concentration of volatile organic compounds is 0.5%, the components are a mixture of pentane, cyclohexene, cyclohexane, cyclohexanol, benzene and cyclohexanone in any proportion) is directly introduced into the buffer tank (2) through a gas inlet (8) after absorption, and the operation is carried out at the temperature of minus 10 ℃. And the gas is discharged from the deoiled gas outlet (9) and enters the first adsorption tower (3) through the gas inlet (11) of the first adsorption tower. The adsorption temperature is-10 ℃, the pressure is 400kPa (absolute pressure), organic matters are adsorbed on the adsorbent after passing through the adsorbent layer in the first adsorption tower (3), oil gas from the gas outlet (12) after adsorption of the organic matters in the first adsorption tower enters the second adsorption tower (4) through the gas inlet (13) of the second adsorption tower for adsorption operation, the adsorption temperature is-30 ℃, the pressure is 380kPa (absolute pressure), the organic matters are adsorbed on the adsorbent after passing through the adsorbent layer in the second adsorption tower (4), and treated gas (nitrogen gas, wherein the total non-methane hydrocarbon content is 20ppm, and the carbon content is 400kPa (absolute pressure)6Compound 4ppm) is discharged from the gas outlet (14) after the second adsorption tower has adsorbed.
And fourthly, when the first adsorption tower (3) is close to saturation, closing the gas inlet (11) of the first adsorption tower of the adsorption tower (3). The first adsorption tower (3) is cut out and is ready for use after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the second adsorption tower (4). After the second step, the gas is discharged from the buffer tank (2) through a deoiled gas outlet (9), enters the second adsorption tower (4) through a gas inlet (13) of the second adsorption tower, organic matters are adsorbed on the adsorbent after passing through an adsorbent layer of the second adsorption tower (4), and the treated gas (nitrogen, wherein the non-methane total hydrocarbon is 40ppm, and the aromatic hydrocarbon is 4ppm) is discharged from a gas outlet (14) after being adsorbed by the second adsorption tower.
And fifthly, when the second adsorption tower (4) is close to saturation, cutting off the second adsorption tower (4) for standby after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the first absorption tower (3), and the steps are repeated.
Example 4
As shown in fig. 1, an absorption tower (1), a buffer tank (2), a first adsorption tower (3) and a second adsorption tower (4) are connected in sequence; liquid hydrocarbon absorbent (boiling point of 200-240 ℃, freezing point of-50 to-35 ℃) is added into the absorption tower from a liquid absorbent adding port (6). Filling an adsorbent (20% of acid clay, 20% of activated carbon fiber and 60% of graphene in mass fraction) in a first adsorption tower (3); the second adsorption tower (4) is filled with adsorbents (90% of carbon nanotubes and 10% of alumina in mass fraction).
Firstly, an absorption tower (1), a buffer tank (2) and a first absorption tower (3) are adopted to carry out series operation. Mixing oil gas (main gas Ar. with volatile organic compounds content of 0.01 vol%; component C)4-C5A mixture of isoparaffin, pyridine, toluene and furan in any proportion) is introduced from a gas inlet (5) containing volatile organic compounds in the absorption tower (1), the absorption temperature is-30 ℃, the pressure is 500kPa (absolute pressure), and the absorption rate is 75%. After being absorbed by the liquid hydrocarbon absorbent, most of oil gas is changed into liquid and is remained in a liquid phase, a small amount of oil gas is led into the buffer tank (2) from the gas outlet (7) of the absorption tower along with the gas through the gas inlet (8) after absorption, the operation is carried out at the temperature of minus 30 ℃, a small amount of oil in the gas is condensed, and the condensed oil is periodically discharged from the condensed liquid outlet (10).
And secondly, gas is discharged from a buffer tank from a deoiled gas outlet (9), enters a first adsorption tower (3) through a first adsorption tower gas inlet (11), the adsorption temperature is 0 ℃, the pressure is 400kPa (absolute pressure), organic matters are adsorbed on an adsorbent after passing through an adsorbent layer in the first adsorption tower (3), and treated gas (Ar, wherein the non-methane total hydrocarbon is 35ppm, and the aromatic hydrocarbon is 3ppm) is discharged from a first adsorption tower adsorption outlet (12).
And thirdly, when the liquid hydrocarbon absorbent in the absorption tower (1) is close to saturation, closing the gas inlet (5) containing the volatile organic compounds in the absorption tower (1), cutting off the absorption tower (1), and desorbing for later use. The operation mode is changed into a series operation between the buffer tank (2), the first adsorption tower (3) and the second adsorption tower (4). Oil gas (0.01% C)4-C5Isoparaffins, pyridines, methanesA mixture of benzene and furan in any proportion) is directly introduced into the buffer tank (2) through the post-absorption gas inlet (8) and operated at-30 ℃. And the gas is discharged from the deoiled gas outlet (9) and enters the first adsorption tower (3) through the gas inlet (11) of the first adsorption tower. The adsorption temperature is-10 ℃, the pressure is 400kPa (absolute pressure), organic matters are adsorbed on the adsorbent after passing through the adsorbent layer in the first adsorption tower (3), oil gas from the gas outlet (12) after adsorption of the organic matters in the first adsorption tower enters the second adsorption tower (4) through the gas inlet (13) of the second adsorption tower for adsorption operation, the adsorption temperature is-20 ℃, the pressure is 350kPa (absolute pressure), the organic matters are adsorbed on the adsorbent after passing through the adsorbent layer in the second adsorption tower (4), and treated gas (Ar) is gas (Ar) in which non-methane total hydrocarbons are 30PPm and C is absolute pressure5The above compound 4PPm) is discharged from the gas outlet (14) after the adsorption of the second adsorption tower.
And fourthly, closing the gas inlet (11) of the first adsorption tower when the first adsorption tower (3) is close to saturation. The first adsorption tower (3) is cut out and is ready for use after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the second adsorption tower (4). Namely, after the second step, the gas is discharged from the buffer tank (2) through a deoiled gas outlet (9), enters the second adsorption tower (4) through a gas inlet (13) of the second adsorption tower, and is adsorbed on the adsorbent after passing through the adsorbent layer of the second adsorption tower (4), and the treated gas (Ar, wherein the non-methane total hydrocarbon is 30PPm, C5The above compound 4ppm) is discharged from the outlet (14) after the second adsorption tower is adsorbed.
And fifthly, when the second adsorption tower (4) is close to saturation, cutting off the second adsorption tower (4) for standby after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the first absorption tower (3), and the steps are repeated.
Example 5
As shown in fig. 1, an absorption tower (1), a buffer tank (2), a first adsorption tower (3) and a second adsorption tower (4) are connected in sequence; liquid hydrocarbon absorbent (boiling point of 220-260 ℃ and freezing point of-40 to-30 ℃) is added into the absorption tower from a liquid absorbent adding port (6). Filling an adsorbent (a molecular sieve with the mass fraction of 3 percent and 97 percent of carbon nano tubes) in a first adsorption tower (3); an adsorbent (50% by mass of carbon nanotubes and 50% by mass of activated carbon fibers) is filled in the second adsorption tower (4).
Firstly, an absorption tower (1), a buffer tank (2) and a first absorption tower (3) are adopted to carry out series operation. Oil gas (the main gas is CO)2Wherein the volume concentration of the volatile organic compounds is 1 percent, the components are octane, ethyl tert-butyl ether, benzene, thiophene and a mixture with the boiling point of 120-140 ℃ organic compounds in any proportion), the gas containing the volatile organic compounds is introduced from a gas inlet (5) of the absorption tower (1), the absorption temperature is 5 ℃, the pressure is 320kPa (absolute pressure), and the absorption rate is 95 percent. After being absorbed by the liquid hydrocarbon absorbent, most of oil gas is changed into liquid and is remained in a liquid phase, a small amount of oil gas is led into the buffer tank (2) from the gas outlet (7) of the absorption tower along with the gas through the gas inlet (8) after absorption, the operation is carried out at the temperature of minus 20 ℃, a small amount of oil in the gas is condensed, and the condensed oil is periodically discharged from the condensed liquid outlet (10).
Secondly, gas is discharged from a gas outlet (9) after deoiling out of the buffer tank and enters a first adsorption tower (3) through a gas inlet (11) of the first adsorption tower, the adsorption temperature is-20 ℃, the pressure is 280kPa (absolute pressure), organic matters are adsorbed on the adsorbent after passing through an adsorbent layer in the first adsorption tower (3), and the treated gas (CO)2Wherein the non-methane total hydrocarbon is 35ppm, the aromatic hydrocarbon is 3ppm), and is discharged from an outlet (12) after being adsorbed by the first adsorption tower;
and thirdly, when the liquid hydrocarbon absorbent in the absorption tower (1) is close to saturation, closing the gas inlet (5) containing the volatile organic compounds in the absorption tower (1), cutting off the absorption tower (1), and desorbing for later use. The operation mode is changed into a series operation between the buffer tank (2), the first adsorption tower (3) and the second adsorption tower (4). Oil gas (the main gas is CO)2Wherein the volume concentration of the volatile organic compounds is 1 percent, the components are octane, ethyl tert-butyl ether, benzene, thiophene and the mixture of organic compounds with the boiling point of 120-. The gas is discharged from a deoiled gas outlet (9) and enters the first adsorption tower (3) through a gas inlet (11) of the first adsorption tower. The adsorption temperature is-20 ℃, the pressure is 300kPa (absolute pressure), and the adsorption solution passes through the first adsorption tower (3)After the adsorbent layer, organic matters are adsorbed on the adsorbent, oil gas discharged from a gas outlet (12) after adsorption of the first adsorption tower enters a second adsorption tower (4) through a gas inlet (13) of the second adsorption tower for adsorption operation, the adsorption temperature is 10 ℃, the pressure is 260kPa (absolute pressure), after passing through the adsorbent layer in the second adsorption tower (4), the organic matters are adsorbed on the adsorbent, and treated gas (CO)2Wherein the non-methane total hydrocarbons are 15ppm, C5The above compound 4ppm) is discharged from the gas outlet (14) after the adsorption in the second adsorption tower.
And fourthly, closing the gas inlet (11) of the first adsorption tower when the first adsorption tower (3) is close to saturation. The first adsorption tower (3) is cut out and is ready for use after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the adsorption tower (4). Namely, after the second step, the gas is discharged from the buffer tank (2) through a deoiled gas outlet (9), enters the second adsorption tower (4) through a gas inlet (13) of the second adsorption tower, and passes through an adsorbent layer of the second adsorption tower (4), organic matters are adsorbed on the adsorbent, and the treated gas (CO)2Wherein the non-methane total hydrocarbons are 15ppm, C5The above compound 4ppm) is discharged from the outlet (14) after the second adsorption tower is adsorbed.
And fifthly, when the second adsorption tower (4) is close to saturation, cutting off the second adsorption tower (4) for standby after desorption operation. The operation mode is changed into the series operation among the absorption tower (1), the buffer tank (2) and the first absorption tower (3), and the steps are repeated.
Claims (7)
1. A system for treating hydrocarbons, comprising: the device comprises an absorption tower (1), a buffer tank (2), two absorption towers, namely a first absorption tower (3) and a second absorption tower (4), wherein a gas inlet (5) containing volatile organic compounds and a liquid absorbent adding port (6) are arranged in the middle of the absorption tower (1), and an absorption tower gas outlet (7) is arranged at the top of the absorption tower; the top of the buffer tank (2) is provided with an absorbed gas inlet (8) and a deoiled gas outlet (9) which are communicated with the gas outlet (7) of the absorption tower, the absorbed gas inlet (8) is also communicated with an inlet pipeline for directly absorbing fresh oil gas, the inlet pipeline is provided with a fourth valve (d), and the bottom of the buffer tank (2) is provided with a condensate outlet (10); the bottom of the first adsorption tower (3) is provided with a first adsorption tower gas inlet (11) communicated with the deoiled gas outlet (9), and the top of the first adsorption tower is provided with a first adsorption tower adsorbed gas outlet (12); the bottom of the second adsorption tower (4) is provided with a second adsorption tower gas inlet (13) communicated with the first adsorption tower adsorbed gas outlet (12), and the top of the second adsorption tower is provided with a second adsorption tower adsorbed gas outlet (14); the absorption tower (1) is connected with the buffer tank (2) in series, the buffer tank (2) is connected with the first adsorption tower (3) and the second adsorption tower (4) in series, and the first adsorption tower (3) is connected with the second adsorption tower (4) in series or in parallel;
a baffle plate is arranged in the middle of the buffer tank (2) so that the gas entering from the gas inlet (8) after absorption has enough residence time in the buffer tank; the operating temperature of the buffer tank (2) is 30-10 ℃ below zero;
the first adsorption tower (3) and the second adsorption tower (4) are filled with easily-regenerated adsorbents, and the easily-regenerated adsorbents contain one or more materials of acid clay, alumina, molecular sieves, activated carbon fibers, carbon nanotubes and graphene;
the method for treating oil and gas by the system comprises the following steps:
a) the absorption tower (1), the buffer tank (2), the first adsorption tower (3) and the second adsorption tower (4) are connected in sequence;
b) adding a liquid hydrocarbon absorbent into the absorption tower (1) from a liquid absorbent adding port (6), and respectively filling the absorbent into the first absorption tower (3) and the second absorption tower (4);
c) firstly, an absorption tower (1), a buffer tank (2) and a first absorption tower (3) are adopted to carry out series operation; introducing gas containing volatile organic compounds from a first valve (a) of a gas introducing port (5) containing the volatile organic compounds of an absorption tower (1), absorbing by a liquid hydrocarbon absorbent, changing most of oil gas into liquid, remaining in a liquid phase, introducing a small amount of oil gas from a third valve (c) of a gas outlet (7) of the absorption tower along with the gas into a buffer tank (2) from a gas inlet (8) after absorption, condensing a small amount of oil in the gas, and periodically discharging the condensed oil from a fifth valve (e) of a condensed liquid outlet (10); d) gas is discharged from the buffer tank (2) from the deoiled gas outlet (9), enters the first adsorption tower (3) through the first adsorption tower gas inlet (11), passes through an adsorbent layer of the first adsorption tower (3), is adsorbed on the adsorbent, and is discharged from a seventh valve (g) of the first adsorption tower adsorbed gas outlet (12) at the top of the first adsorption tower (3) to reach the standard;
e) when the liquid hydrocarbon absorbent of the absorption tower (1) is close to saturation, closing a first valve (a) of a gas inlet (5) containing volatile organic compounds of the absorption tower (1), a second valve (b) of a gas outlet (7) of the absorption tower and a third valve (c), cutting off the absorption tower (1), and desorbing for later use; changing the operation mode into the series operation among the buffer tank (2), the first adsorption tower (3) and the second adsorption tower (4); introducing unabsorbed oil gas into a buffer tank (2) through a fourth valve (d) and an absorbed gas inlet (8) directly, discharging the oil gas from an deoiled gas outlet (9), entering a first adsorption tower (3) through a first adsorption tower gas inlet (11), allowing the oil gas from an eighth valve (h) of a gas outlet (12) adsorbed by the first adsorption tower to enter a second adsorption tower (4) through a second adsorption tower gas inlet (13) for adsorption operation, and discharging the gas from a gas outlet (14) adsorbed by the second adsorption tower to reach the standard;
f) when the first adsorption tower (3) is close to saturation, closing a ninth valve (i) of a gas inlet (11) of the first adsorption tower and a seventh valve (g) and an eighth valve (h) of a gas outlet (12) after adsorption of the first adsorption tower; cutting out the first adsorption tower (3), and performing desorption operation for later use; the series operation of the absorption tower (1), the buffer tank (2) and the second adsorption tower (4) is changed, namely, after the gas is deoiled, a gas outlet (9) is discharged from the buffer tank (2) and enters the second adsorption tower (4) through a sixth valve (f) and a second adsorption tower gas inlet (13), after passing through an adsorbent layer of the second adsorption tower (4), organic matters are adsorbed on an adsorbent, and the adsorbed gas is discharged from a second adsorption tower gas outlet (14) at the top of the second adsorption tower (4) and is discharged after reaching the standard;
g) when the second adsorption tower (4) is close to saturation, the second adsorption tower (4) is cut out and is subjected to desorption operation for later use; the operation mode is changed to: the absorption tower (1), the buffer tank (2) and the first absorption tower (3) are operated in series, and the steps c) to g) are repeated.
2. The system for treating hydrocarbons according to claim 1, wherein: when the absorption tower (1) executes the absorption operation, the temperature is 30-10 ℃ below zero, the absolute pressure is 120-500KPa, and the absorption rate is 75-95%.
3. The system for treating hydrocarbons according to claim 1, wherein: when the first adsorption tower (3) or the second adsorption tower (4) executes the adsorption operation, the temperature is 30-10 ℃ below zero, and the absolute pressure is 100-480 KPa; the adsorption effect is as follows: the content of non-methane total hydrocarbon in the inert gas is less than 50ppm, and the content of aromatic hydrocarbon compound is less than 4 ppm.
4. The system for treating hydrocarbons according to claim 1, wherein: the main body of the gas containing the volatile organic compounds is inert gas, wherein the volume concentration of the volatile organic compounds is 0.01-2%, and the components are organic compounds with the molecular weight of 26-150.
5. The system for treating hydrocarbons according to claim 1, wherein: the absorption tower (1) is filled with liquid hydrocarbon absorbent, the boiling point of which is 200-300 ℃, and the freezing point of which is minus 10 ℃ to minus 50 ℃.
6. The system for treating hydrocarbons according to claim 1, wherein: the gas inlet of the absorption tower (1) containing volatile organic compounds enters from the middle of the absorption tower (1) and extends to the bottom so as to ensure that oil gas entering the absorption tower (1) has sufficient contact time with the liquid hydrocarbon absorbent.
7. The system for treating oil and gas according to claim 1, wherein the baffle in the middle of the buffer tank (2) is a vertical baffle.
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