CN103252107A - Flare gas recycling method and device for high-boiling-point material with normal pressure boiling point being more than or equal to 80 DEG C - Google Patents
Flare gas recycling method and device for high-boiling-point material with normal pressure boiling point being more than or equal to 80 DEG C Download PDFInfo
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- CN103252107A CN103252107A CN2013101373137A CN201310137313A CN103252107A CN 103252107 A CN103252107 A CN 103252107A CN 2013101373137 A CN2013101373137 A CN 2013101373137A CN 201310137313 A CN201310137313 A CN 201310137313A CN 103252107 A CN103252107 A CN 103252107A
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Abstract
The invention discloses a flare gas recycling method and a recycling device for a high-boiling-point material with a normal pressure boiling point being more than or equal to 80 DEG C. An emptying material at the top of a fractionation or rectification tower is fed into a cold material; the cold material is loaded in a cold tank; the volume of the cold tank is 50-70 percent of the tank capacity of the cold tank, preferably 60 percent of the tank capacity of the cold tank; the emptying material is cooled and condensed by the cold material; non-condensed gas enters a cold bath type water cooler so as to be condensed again; the material discharged from the cold bath type water cooler enters a gas-liquid separator, so that a liquid phase is recycled; and a gas phase enters a flare system. By the flare gas recycling method for the high-boiling-point material with the normal pressure boiling point being more than or equal to 80 DEG C, the flare gas recycling rate is high (nearly 100 percent); and the method has the characteristics of small investment, low energy consumption, high efficiency and convenience in operation, and the environment pollution is reduced.
Description
Technical field:
The present invention relates to high boiler material process for recovering torch gas and the retracting device of atmospheric boiling point in a kind of petrochemical production process 〉=80 ℃.Also can be used for other and relate to the recovery of high temperature heavy torch gas.
Technical background:
In petrochemical industry, because feed separation mostly adopts the method for fractionation or rectifying, and, damage incidents for avoiding the equipment superpressure in the state of accident, the safety vent gas flow of fractionation or rectifying column very big (being generally 3-18 overhead product doubly) and temperature higher (〉=100 ℃).
Petroleum chemical enterprise adopts the mode of the torch burning emptying of directly setting fire to handle these safety vent gases at present.Direct result is: resource is burnt in vain, causes waste, has increased carbon emission again simultaneously, causes environmental pollution.Retrieve technical data and document that relevant torch gas reclaims, also do not had the research report of this respect both at home and abroad.
Summary of the invention:
The purpose of this invention is to provide a kind of petrochemical industry produce in the high boiler material process for recovering torch gas of atmospheric boiling point 〉=80 ℃.It can reclaim safety vent gas effectively.Have that investment is little, energy consumption is low, efficient is high, reduce environmental pollution, convenience operation.
Another object of the present invention is to provide the high boiler material flare gas recovery of a kind of atmospheric boiling point 〉=80 ℃.
Purpose of the present invention is achieved through the following technical solutions:
The high boiler material process for recovering torch gas of a kind of atmospheric boiling point 〉=80 ℃ feeds the emptying material of fractionation or rectifying tower top in the cold burden, and described cold burden is loaded in cold jar, and volume is 50% ~ 70% jar of appearance, is preferably 60% jar of appearance; The emptying material is through cold burden cooling condensation, and uncooled gas enters cryostat formula water cooler and continues condensation, goes out the material of cryostat formula water cooler, enters gas-liquid separator, and liquid phase reclaims, and gas phase enters flare system again.
Material or the emptying material itself of described cold burden for dissolving each other fully with described emptying material.
The amount of described cold burden is carried out energy balance by 5 minutes emptying material gas flow, and cold burden rises to 70 ℃ from 40 ℃; The cold burden amount is determined by following formula:
M?=?V×〔C
P1×（T－T
1）+C
P2×(T
1-70)+△H〕/(360×C
P3)
In the formula:
M-required cold burden amount, Kg;
V-emptying material flow rate, Kg/h;
T-emptying material exhaust temperature, ℃;
T
1-emptying material condensation temperature, ℃;
C
P1The avergae specific heat of-emptying material between T and T1, KJ/Kg. ℃;
C
P2The avergae specific heat of-emptying material between T1 and 70 ℃, KJ/Kg. ℃;
C
P3The avergae specific heat of-cold material between 70 ℃ and 40 ℃, KJ/Kg. ℃;
The latent heat of phase change of △ H-emptying material, KJ/Kg.
Described cold jar is that size is determined in 0.5 ~ 0.7 calculating by load factor N, and preferred load factor N is 0.6;
Cold tank volume:
R=M×r
c/N
In the formula:
The required cold tank volume of R--, m
3
The required cold burden amount of M--, Kg;
r
c--the specific volume of cold burden in the time of 70 ℃, m
3/ Kg;
N-load factor.
Described cryostat formula water cooler carries out energy balance by 2 minutes emptying material gas flow of condensation and determines heat exchange area, and cooling water rises to 45 ℃ from 30 ℃; Cryostat formula water cooler heat exchange area amount is determined by following formula:
A=?V×〔C
P1×（T－T
1）+△H〕/(K×△T
m)
In the formula:
The required heat exchange area of A--, m
2
V--emptying material flow rate, Kg/h;
T--emptying material exhaust temperature, ℃;
T
1--emptying material condensation temperature, ℃;
C
P1--the avergae specific heat of emptying material between T and T1, KJ/Kg. ℃;
The latent heat of phase change of △ H--emptying material, KJ/Kg;
The K--overall heat-transfer coefficient, KJ/m
2.h. ℃;
△ T
m--the emptying material drops to T from T ℃
1℃, water is from 30 ℃ of logarithmic mean temperature difference (LMTD)s that are raised to 45 ℃, ℃.
The high boiler material flare gas recovery of a kind of atmospheric boiling point 〉=80 ℃, drop out line and gas-liquid separator after cold jar, the cold back drop out line that comprises high temperature high boiler material drop out line and be linked in sequence, cryostat formula water cooler, the water-cooled, an end of described high temperature high boiler material drop out line are inserted under the cold burden liquid level in cold jar.
Described cold jar in the injection rate of cold burden be jar hold 50% ~ 70%, be preferably 60%, an end of described high temperature high boiler material drop out line is inserted into 700 ~ 900mm under the cold burden liquid level in the cold jar, is preferably 800mm.
Described cold jar is provided with for the recovery liquid and the hot stockline that feed the cold burden line of cold burden and be used for cold jar of interior cold burden discharged in cold jar.
Gas phase in the described gas-liquid separator is communicated with into flare system by the normal temperature drop out line that is located at the gas-liquid separator top, and liquid phase reclaims by the emptying lime set line that is located at the gas-liquid separator bottom.
The process that adopts above-mentioned device to reclaim torch gas is: feed the emptying material in fractionation or the rectifying tower top in the cold burden that is loaded into cold jar by high temperature high boiler material drop out line, the emptying material is by the cold burden condensation of lowering the temperature, uncooled gas enters cryostat formula water cooler and continues condensation, go out the material of cryostat formula water cooler, enter gas-liquid separator, liquid phase reclaims, and gas phase enters flare system again.
The other end of the high temperature high boiler material drop out line that one end is communicated with fractionation or rectifying tower top inserts one and is equipped with 50% ~ 70% jar all the time and holds in cold jar of cold burden, and insertion depth is 700 ~ 900mm under the liquid level, forms fluid-tight.Material or the emptying material itself of cold burden in the container for dissolving each other fully with the emptying material.Emptying material cooling condensation, recovery, the cold burden heat absorption heats up, and does not have the gas of condensation to be picked out via cold back drop out line by container top, enter cryostat formula water cooler and continue condensation, go out the material of cryostat formula water cooler, enter gas-liquid separator, liquid phase reclaims, and gas phase enters flare system again.
Normal pressure of the present invention is to well known to a person skilled in the art a standard atmospheric pressure, i.e. 100KPa or 0.1MPa.
Beneficial effect of the present invention:
The high boiler material process for recovering torch gas of atmospheric boiling point of the present invention 〉=80 ℃ reclaims torch gas, and rate of recovery height (near 100%) has that investment is little, energy consumption is low, efficient is high, reduce environmental pollution, convenience operation.
Description of drawings
Fig. 1 is the high boiler material flare gas recovery structure chart of atmospheric boiling point of the present invention 〉=80 ℃.
The specific embodiment:
The following examples will be further detailed the present invention, but therefore not limit the present invention.
Embodiment 1: the high boiler material flare gas recovery of atmospheric boiling point 〉=80 ℃
The high boiler material flare gas recovery of a kind of atmospheric boiling point 〉=80 as shown in Figure 1 ℃: comprise drop out line 9 and gas-liquid separator 10 after high temperature high boiler material drop out line 1 and cold jar 3 of being linked in sequence, cold back drop out line 4, cryostat formula water cooler 8, the water-cooled, an end of described high temperature high boiler material drop out line 1 is inserted under the cold burden liquid level in cold jar 3.In described cold jars 3 the injection rate of cold burden be jar hold 60%, an end of described high temperature high boiler material drop out line 1 is inserted into 800mm under the cold burden liquid level in the cold jar 3.Described cold jar 3 is provided with for the recovery liquid and the hot stockline 5 that feed the cold burden line 2 of cold burden and be used for cold jar 3 interior cold burden discharged in cold jar 3.Gas phase in the described gas-liquid separator 10 is communicated with to go into flare system by the normal temperature drop out line 11 that is located at gas-liquid separator 10 tops, and liquid phase reclaims by the emptying lime set line 12 that is located at gas-liquid separator 10 bottoms.The cycling hot waterline 7 that passes through to be located at the circulating water line 6 of bottom and to be located at top of described cryostat formula water cooler 8 carries out cooling water circulation.
Embodiment 2
The safety vent material is 165 ℃ gas paraxylene, 30 tons/hour, adopts mixing 〉=C8
+Aromatic hydrocarbons is cold burden.Adopt embodiment 1 described device to reclaim torch gas: the emptying material is fed in cold jar 3 that 60% jar of appearance cold burden is housed by high temperature high boiler material drop out line 1, and insertion depth is 800mm under the liquid level, forms fluid-tight.The emptying material is by the cold burden condensation of lowering the temperature, and uncooled gas enters cryostat formula water cooler 8 and continues condensations, goes out the material of cryostat formula water cooler 8, enters gas-liquid separator 10, and liquid phase reclaims, and gas phase enters flare system again.
The amount of described cold burden is carried out energy balance by 5 minutes emptying material gas flow, and cold burden rises to 70 ℃ from 40 ℃; The cold burden amount is determined by following formula:
M?=?V×〔C
P1×（T－T
1）+C
P2×(T
1-70)+△H〕/(360×C
P3)
In the formula:
M-required cold burden amount, Kg;
V-emptying material flow rate, Kg/h;
T-emptying material exhaust temperature, ℃;
T
1-emptying material condensation temperature, ℃;
C
P1The avergae specific heat of-emptying material between T and T1, KJ/Kg. ℃;
C
P2The avergae specific heat of-emptying material between T1 and 70 ℃, KJ/Kg. ℃;
C
P3The avergae specific heat of-cold material between 70 ℃ and 40 ℃, KJ/Kg. ℃;
The latent heat of phase change of △ H-emptying material, KJ/Kg.
Described cold jar is that size is determined in 0.6 calculating by load factor N;
Cold tank volume:
R=M×r
c/N
In the formula:
The required cold tank volume of R--, m
3
The required cold burden amount of M--, Kg;
r
c--the specific volume of cold burden in the time of 70 ℃, m
3/ Kg;
N-load factor.
Described cryostat formula water cooler carries out energy balance by 2 minutes emptying material gas flow of condensation and determines heat exchange area, and cooling water rises to 45 ℃ from 30 ℃; Cryostat formula water cooler heat exchange area amount is determined by following formula:
A=?V×〔C
P1×（T－T
1）+△H〕/(K×△T
m)
In the formula:
The required heat exchange area of A--, m
2
V--emptying material flow rate, Kg/h;
T--emptying material exhaust temperature, ℃;
T
1--emptying material condensation temperature, ℃;
C
P1--the avergae specific heat of emptying material between T and T1, KJ/Kg. ℃;
The latent heat of phase change of △ H--emptying material, KJ/Kg;
The K--overall heat-transfer coefficient, KJ/m
2.h. ℃;
△ T
m--the emptying material drops to T from T ℃
1℃, water is from 30 ℃ of logarithmic mean temperature difference (LMTD)s that are raised to 45 ℃, ℃.
The result: need 24.5 tons of cold burdens, cold jar is of a size of Φ 2800 * 7600, cryostat formula water cooler heat exchange area 540m
2
Reclaim the result: the rate of recovery 100% of 165 ℃ gas paraxylene, can reclaim a large amount of paraxylene every year and carry out recycling, save cost, reduce discharge amount of exhaust gas, reduce environmental pollution.
Embodiment 3:
The safety vent material is 180 ℃ gas first and second benzene, propyl benzene, 20 tons/hour, adopts mixing 〉=C9
+Aromatic hydrocarbons is cold burden, adopts embodiment 1 described device to reclaim torch gas.The amount of described cold burden is carried out energy balance by 5 minutes emptying material gas flow, and cold burden rises to 70 ℃ from 40 ℃; Described cold jar is that size is determined in 0.6 calculating by load factor N; Described cryostat formula water cooler carries out energy balance by 2 minutes emptying material gas flow of condensation and determines heat exchange area, and cooling water rises to 45 ℃ from 30 ℃; Computing formula is with embodiment 2.The result: need 16.3 tons of cold burdens, cold jar is of a size of Φ 2400 * 7200, cryostat formula water cooler heat exchange area 285m
2
Reclaim the result: 180 ℃ gas first and second benzene, the rate of recovery of propyl benzene be near 99.7%, can reclaim the first and second a large amount of benzene every year, propyl benzene carries out recycling, saves cost, reduces discharge amount of exhaust gas, reduces environmental pollution.
Embodiment 4:
The safety vent material is 260 ℃ gas kerosene component, and 15 tons/hour, employing diesel oil is cold burden, adopts embodiment 1 described device to reclaim torch gas.The amount of described cold burden is carried out energy balance by 5 minutes emptying material gas flow, and cold burden rises to 70 ℃ from 40 ℃; Described cold jar is that size is determined in 0.6 calculating by load factor N; Described cryostat formula water cooler carries out energy balance by 2 minutes emptying material gas flow of condensation and determines heat exchange area, and cooling water rises to 45 ℃ from 30 ℃; Computing formula is with embodiment 2.The result: need 14.8 tons of cold burdens, cold jar is of a size of Φ 2400 * 7200, cryostat formula water cooler heat exchange area 168 m
2
Reclaim the result: the rate of recovery 99.6% of 260 ℃ gas kerosene component, can reclaim a large amount of kerosene component every year and carry out recycling, save cost, reduce discharge amount of exhaust gas, reduce environmental pollution.
Adopt method and apparatus of the present invention, can reclaim a large amount of safety vent gases (rate of recovery height is near 100%) effectively, and recycle, be conducive to energy savings.Have that investment is little, energy consumption is low, efficient is high, reduce environmental pollution, convenience operation.
Claims (9)
1. the high boiler material process for recovering torch gas of atmospheric boiling point 〉=80 ℃, it is characterized in that: the emptying material of fractionation or rectifying tower top is fed in the cold burden, and described cold burden is loaded in cold jar, and volume is 50% ~ 70% jar of appearance, is preferably 60% jar of appearance; The emptying material is through cold burden cooling condensation, and uncooled gas enters cryostat formula water cooler and continues condensation, goes out the material of cryostat formula water cooler, enters gas-liquid separator, and liquid phase reclaims, and gas phase enters flare system again.
2. the high boiler material process for recovering torch gas of atmospheric boiling point according to claim 1 〉=80 ℃ is characterized in that: material or the emptying material itself of described cold burden for dissolving each other fully with described emptying material.
3. the high boiler material process for recovering torch gas of atmospheric boiling point according to claim 1 〉=80 ℃, it is characterized in that: the amount of described cold burden is carried out energy balance by 5 minutes emptying material gas flow, and cold burden rises to 70 ℃ from 40 ℃; The cold burden amount is determined by following formula:
M?=?V×〔C
P1×（T－T
1）+C
P2×(T
1-70)+△H〕/(360×C
P3)
In the formula:
M-required cold burden amount, Kg;
V-emptying material flow rate, Kg/h;
T-emptying material exhaust temperature, ℃;
T
1-emptying material condensation temperature, ℃;
C
P1The avergae specific heat of-emptying material between T and T1, KJ/Kg. ℃;
C
P2The avergae specific heat of-emptying material between T1 and 70 ℃, KJ/Kg. ℃;
C
P3The avergae specific heat of-cold material between 70 ℃ and 40 ℃, KJ/Kg. ℃;
The latent heat of phase change of △ H-emptying material, KJ/Kg.
4. the high boiler material process for recovering torch gas of atmospheric boiling point according to claim 1 〉=80 ℃ is characterized in that: described cold jar is 0.5 ~ 0.7 to calculate and determine size by load factor N, and preferred load factor N is 0.6;
Cold tank volume:
R=M×r
c/N
In the formula:
The required cold tank volume of R--, m
3
The required cold burden amount of M--, Kg;
r
c--the specific volume of cold burden in the time of 70 ℃, m
3/ Kg;
N-load factor.
5. the high boiler material process for recovering torch gas of atmospheric boiling point according to claim 1 〉=80 ℃, it is characterized in that: described cryostat formula water cooler carries out energy balance by 2 minutes emptying material gas flow of condensation and determines heat exchange area, and cooling water rises to 45 ℃ from 30 ℃; Cryostat formula water cooler heat exchange area amount is determined by following formula:
A=?V×〔C
P1×（T－T
1）+△H〕/(K×△T
m)
In the formula:
The required heat exchange area of A--, m
2
V--emptying material flow rate, Kg/h;
T--emptying material exhaust temperature, ℃;
T
1--emptying material condensation temperature, ℃;
C
P1--the avergae specific heat of emptying material between T and T1, KJ/Kg. ℃;
The latent heat of phase change of △ H--emptying material, KJ/Kg;
The K--overall heat-transfer coefficient, KJ/m
2.h. ℃;
△ T
m--the emptying material drops to T from T ℃
1℃, water is from 30 ℃ of logarithmic mean temperature difference (LMTD)s that are raised to 45 ℃, ℃.
6. the high boiler material flare gas recovery of atmospheric boiling point 〉=80 ℃, it is characterized in that: comprise drop out line (9) and gas-liquid separator (10) after high temperature high boiler material drop out line (1) and cold jar (3) that are linked in sequence, cold back drop out line (4), cryostat formula water cooler (8), the water-cooled, an end of described high temperature high boiler material drop out line (1) is inserted under the cold burden liquid level in the cold jar (3).
7. the high boiler material flare gas recovery of atmospheric boiling point according to claim 1 〉=80 ℃, it is characterized in that: in described cold jar (3) injection rate of cold burden for jar hold 50% ~ 70%, an end of described high temperature high boiler material drop out line (1) is inserted into 700 ~ 900mm under the cold burden liquid level in cold jar (3).
8. the high boiler material flare gas recovery of atmospheric boiling point according to claim 1 〉=80 ℃ is characterized in that: described cold jar (3) are provided with for feeding the cold burden line (2) of cold burden and be used for recovery liquid and hot stockline (5) with cold jar (3) interior cold burden discharge in cold jar (3).
9. the high boiler material flare gas recovery of atmospheric boiling point according to claim 1 〉=80 ℃, it is characterized in that: the gas phase in the described gas-liquid separator (10) is communicated with to go into flare system by the normal temperature drop out line (11) that is located at gas-liquid separator (10) top, and liquid phase reclaims by the emptying lime set line (12) that is located at gas-liquid separator (10) bottom.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310137313.7A CN103252107B (en) | 2013-04-18 | 2013-04-18 | The high boiler material process for recovering torch gas of a kind of atmospheric boiling point >=80 DEG C and retracting device |
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|---|---|---|---|
| CN201310137313.7A CN103252107B (en) | 2013-04-18 | 2013-04-18 | The high boiler material process for recovering torch gas of a kind of atmospheric boiling point >=80 DEG C and retracting device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111692895A (en) * | 2019-03-13 | 2020-09-22 | 惠生工程（中国）有限公司 | Cold torch gas liquid separating, vaporizing and heating system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111692895A (en) * | 2019-03-13 | 2020-09-22 | 惠生工程（中国）有限公司 | Cold torch gas liquid separating, vaporizing and heating system |
| CN111692895B (en) * | 2019-03-13 | 2022-06-14 | 惠生工程（中国）有限公司 | Cold torch gas liquid separating, vaporizing and heating system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103252107B (en) | 2015-11-18 |
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