CN101306259A - High-pressure and low-temperature condensing recovery method of volatile organic steam in oil gas - Google Patents
High-pressure and low-temperature condensing recovery method of volatile organic steam in oil gas Download PDFInfo
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- CN101306259A CN101306259A CNA2008100330398A CN200810033039A CN101306259A CN 101306259 A CN101306259 A CN 101306259A CN A2008100330398 A CNA2008100330398 A CN A2008100330398A CN 200810033039 A CN200810033039 A CN 200810033039A CN 101306259 A CN101306259 A CN 101306259A
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Abstract
The invention relates to a low-temperature condensation recycling method for steam of volatile organic compounds, in particular to a pressurized low-temperature condensation recycling method for the steam of the volatile organic compounds in oil gas. The pressurized low-temperature condensation recycling method of the steam of the volatile organic compounds in the oil gas firstly utilizes a gas compressor to carry out pumping and pressurization to the steam of the volatile organic compounds overflowed from an oil storage tank, then the organic compounds with high boiling points are liquefied in a cooler, the steam liquid of the organic compounds after liquefying is discharged from the bottom part of a gas storage tank and enters the oil storage tank for recycling, the liquefied steam of the organic compounds is then sent to a gas separator, the liquid is discharged from the bottom part of the separator and enters the oil storage tank for recycling, the steam enters a low-temperature steam trap to be condensed into the liquid and then enters the oil storage tank for recycling after being discharged, and the rest is discharged into the atmosphere. The recycling method of the invention is safe and reliable, the operation is convenient, the structure of the device is simple, and the production is convenient.
Description
Technical field
The present invention relates to the cryogenic temperature condensation recovery method of volatile organic steam, relate in particular to the high-pressure and low-temperature condensing recovery method of volatile organic steam in the oil gas.
Background technology
In petrol delivery, sale, storing link, exist the situation of discharging high-concentration gasoline steam (being called for short " oil gas ") in atmosphere, seriously polluted the healthy of atmospheric environment and harm people.For reclaiming this part gasoline vapor, the reclaimer on absorption process, absorption method, membrane separation process, condensation method, the oxidizing process basis has appearred being based upon.
Extensive investigations were once done to the gasoline vapor reclaimer by Fushun Petrochemical Research Institute of SINOPEC, and the related personnel also adopts condensation method to do deep research to reclaiming gasoline vapor, and result of study is:
-73 ℃ condensation temperature can reclaim in the oil gas 90% hydrocarbons;
-80 ℃ condensation temperature can reclaim the hydrocarbons more than 90% in the oil gas, control exhaust emissions concentration≤50g/m
3
-95 ℃ condensation temperature can reclaim in the oil gas 95% hydrocarbons, control exhaust emissions concentration≤35g/m
3
-110 ℃ condensation temperature can reclaim in the oil gas 98% hydrocarbons, control exhaust emissions concentration≤25g/m
3
-120 ℃ condensation temperature can reclaim the hydrocarbons more than 98% in the oil gas, control exhaust emissions concentration≤13.4g/m
3
Chinese patent CN89206893.0 " oil gas condensation retracting device " discloses gasoline vapor carry out indirect heat exchange with-2 ℃ sodium chloride solution after, wherein part composition liquefaction and being recovered is coagulated oil gas and is discharged in the air.With regard to the control atmosphere pollution, the effect of this device is very poor, does not reach control exhaust emissions concentration≤25g/m
3Limit value.
Chinese patent CN01115516.7 " Gu media zones cold-storage/condensation reclaims method of oil gas and solvent naphtha " discloses: in 〉=-70 ℃ general cold scope, and the method for condensation liquefaction gasoline vapor.This method adopts at normal temperatures with the calcium chloride dehydration, finishes the technology that oil gas liquefaction is reclaimed under 〉=-70 ℃ temperature, " reaches exhaust quality concentration≤35g/m
3" effect.But, has only mass concentration≤25g/m by present GB 20952-2007 and GB20592-2007 regulation
3Oil gas tail gas, just allow directly to be discharged in the atmosphere.
Chinese patent CN200620078066.3 " condensing type oil gas retracting device " discloses a kind of " rate of recovery 〉=95%, exhaust of oil concentration≤25g/m
3", utilize the complex method of " condensation+charcoal absorption " to reclaim gasoline vapor, and utilize the vavuum pump device attached active carbon desorption.
The flow process that this device reclaims gasoline vapor is:
A. finish in condensation chamber: oil gas dehydration and oil gas liquefy, temperature 〉=-70 ℃;
B. in charcoal canister, finish: the recovery of lighter hydrocarbons and the discharging of on-condensible gas, temperature 〉=-70 ℃.
The top outlet of this device condensation chamber is unique passage that gas and liquid flow out condensation chamber.
Active carbon is as a kind of adsorbent, has selectivity for the absorption of gas or vapour mixture.The adsorption capacity of active carbon, with the reducing and reduce of the molecular weight of hydrocarbon, the hydrocarbon of HMW can cement out the low hydrocarbon of molecular weight from active carbon, and referring to table 1, heavy hydrocarbon is easy to absorption and but is difficult for desorb, makes the activity of active carbon be difficult for recovering.
The molecular weight of table 1 part hydrocarbon
| Title | Molecular weight | Title | Molecular weight |
| Ethylbenzene | 106.169 | Ethanol | 46.069 |
| Toluene | 92.141 | Propane | 44.097 |
| Benzene | 78.115 | Propylene | 42.081 |
| Pentane | 72.151 | Methyl alcohol | 32.042 |
| Amylene | 70.135 | Ethane | 30.070 |
| Butane | 58.124 | Ethene | 28.054 |
| Butylene | 56.108 | Methane | 16.043 |
The defective of this patented technology is:
1, the condensation chamber bottom does not have liquid outlet, is unfavorable for that the oil gas composition that liquefies is in time recycled.
2, gas and liquid are all discharged unreasonable structure from the same position at condensation chamber top.
Summary of the invention
The object of the present invention is to provide the high-pressure and low-temperature condensing recovery method of volatile organic steam in a kind of oil gas, this method adopts the technology that increases oil-air pressure and cryogenic temperature condensation oil gas, by improving the saturated vapor pressure of oil gas, oil gas is liquefied being higher than under the temperature of atmospheric boiling point, this method is safe and reliable, easy to operate, apparatus structure is simple, and is easy to make.
The present invention is achieved in that the high-pressure and low-temperature condensing recovery method of volatile organic steam in a kind of oil gas, at first utilize gas compressor that the volatile organic steam that overflows in oil storage tank is aspirated supercharging, in aftercooler, make high boiling point organic compound liquefaction then, organic steam liquid after the liquefaction is discharged through the air accumulator bottom and is entered the oil storage tank recovery, organic steam after the liquefaction is behind gas separator, liquid is discharged through the separator bottom and is entered the oil storage tank recovery, discharge entered the oil storage tank recovery after steam entered and condensed into liquid in the Low Temperature Steam trap, and surplus is disposed in the atmosphere.
When described Low Temperature Steam trap was collected organic steam, operating temperature was not less than-95 ℃, operating pressure and is not higher than 1.0MPa; Preferably, when the Low Temperature Steam trap was collected organic steam, operating temperature was not less than-75 ℃, operating pressure and is not higher than 0.85MPa; The vapor stream temperature of aftercooler outlet is not higher than 40 ℃, i.e. the vapor stream temperature of aftercooler outlet is not higher than environment temperature.
The present invention has adopted the technology that increases oil-air pressure and cryogenic temperature condensation oil gas, by improving the saturated vapor pressure of oil gas, oil gas is liquefied being higher than under the temperature of atmospheric boiling point.Promptly at first adopt gas compressor that volatile organic steam is aspirated supercharging, in aftercooler, discharge the most heat of compression then, make high boiling point organic compound liquefaction, again in the Low Temperature Steam trap to the volatile organic steam recovery of condensing fully, liquid heavy hydrocarbon is discharged from vapour storage tank, liquid light hydrocarbon is discharged from the Low Temperature Steam trap, does not contain C in the discharge tail gas
2Method of the present invention is safe and reliable, and is easy to operate, is convenient to reclaim the lighter hydrocarbons in the gasoline vapor, and apparatus structure is simple, and is easy to make, safeguards simple.
Description of drawings
Fig. 1 is applied to reclaim the schematic flow sheet of gas station's gasoline vapor for the present invention.
The specific embodiment
The invention will be further described below in conjunction with the drawings and specific embodiments.
Referring to Fig. 1, the high-pressure and low-temperature condensing recovery method of volatile organic steam in the oil gas of the present invention is first with the organic steam supercharging, then cooling, cryogenic temperature condensation again.Its rationale is " Van der Waals equation ":
In the formula:
V: gas volume
P: gas pressure intensity
T: absolute temperature
R: gas constant
A and b are as coefficient, and value is by test determination.
Below be that example describes method of the present invention to reclaim gas station's gasoline vapor.
Referring to Fig. 1, oil truck before oil storage tank 1 (be positioned at underground, also claim ground tank) emptying, is connected the power supply of Cryo Refrigerator 6 in the gas station earlier, makes Cryo Refrigerator 6 according to the program operation of setting, with the low temperature that keeps Low Temperature Steam trap 7 to be in about-75 ℃.
During emptying, earlier the gasoline efferent duct is connected on the oil-in 12, opens hand-operated valve V12, gasoline just flows in the oil storage tank 1.Along with gasoline liquid constantly enters, the liquid level in the oil storage tank 1 constantly raises, and saturated vapor pressure also constantly raises on the liquid level.Explosion-proof type electro connecting pressure gauge P1 on being installed in pipeline detects pressure and has reached when showing to go up the upper pressure limit value of setting, the working power of the gas compressor 2 in the gasoline vapor retracting device is connected automatically, and gas compressor 2 beginnings are with the steam in the constant speed extraction oil storage tank 1.Explosion-proof solenoid valve V12A and gas compressor 2 link.
Explosion-proof solenoid valve V57A, hand-operated valve V57B, the effect of check valve V57C is to make to enter the force value that gasoline vapor in aftercooler 3, vapour storage tank 4, the gas-liquid separator 5 maintains setting.In the present embodiment, setting value is 0.85MPa.
The high-pressure and high-temperature steam that gas compressor 2 is discharged enters in the aftercooler 3 by the road, and by air or be water-cooled to+below 40 ℃, enter vapour storage tank 4 by the road, environment temperature is generally+below 40 ℃.At this moment, in the vapor stream of high normal pressure and temperature some high boiling volatile organic steam formed liquid because of cooling.These liquid major parts are trapped in the vapour storage tank 4, and fraction is separated in gas-liquid separator 5 by the road with vapor stream.
Electro connecting pressure gauge P2 is installed on the pipeline of gas separator 5 delivery outlets, and its effect is the keying that control is installed in the explosion-proof solenoid valve V57A on this pipeline.
Cooling stage is not liquefied, and is lower boiling high steam fluid comparatively speaking, by the road, behind explosion-proof solenoid valve V57A, the hand-operated valve V57B, enter in the Low Temperature Steam trap 7.
The effect of Cryo Refrigerator 6 is the temperature that reduce Low Temperature Steam trap 7, and provides enough colds to keep the operating temperature of setting.Low Temperature Steam trap 7 is when liquefaction low-boiling-point organic compound steam, and the fluctuation degree of its operating temperature can maintain in 1 ℃.When the Low Temperature Steam trap was collected organic steam, its operating temperature was not less than-95 ℃, operating pressure and is not higher than 1.0MPa; Preferable be chosen as operating temperature and be not less than-75 ℃, operating pressure and be not higher than 0.85MPa, present embodiment adopts preferable selection.Organic steam tail gas is discharged through magnetic valve V70A and hand-operated valve V70B from Low Temperature Steam trap 7.
In said process, the fluid of the volatile organic steam of flow through vapour storage tank 4 and gas-liquid separator 5, its temperature is 40 ℃, pressure is 0.85MPa.Gasoline vapor with the recovery gas station is an example, and wherein 90% water vapour is liquefied, and referring to table 2, table 3, and the charcoal number is C
4And C
4Above high-boiling hydrocarbon all liquefies, referring to table 4, table 5, and by vapour storage tank 4 and the separated recovery in gas-liquid separator 5 bottoms.
During table 2 humid air character air pressure P=0.1013MPa
| Air themperature (℃) | Saturated air water capacity (g/kg) | Saturated air density (kg/m 3) |
| 20 | 14.7 | 1.195 |
| 30 | 27.2 | 1.146 |
| 40 | 48.8 | 1.097 |
| 50 | 86.2 | 1043 |
During table 3 humid air character air pressure P=0.1013MPa
| Air themperature (℃) | Saturated air water capacity (g/kg) | Saturated air density (kg/m 3) |
| 20 | 1.824 | 9.497 |
| 30 | 3.319 | 9.175 |
| 40 | 5.794 | 8.869 |
| 50 | 9.752 | 8.574 |
The flow through fluid of volatile organic steam of Low Temperature Steam trap 7, temperature is-75 ℃, pressure is 0.85MPa.Wherein the charcoal number is C
2And C
2Above low boiling point hydrocarbon is liquefied, referring to table 4, table 5, by the separated recovery in Low Temperature Steam trap 7 bottoms.
Shown in the table 4, ethene is at 7.68 atmospheric pressure, below-56 ℃, and recovery just can be liquefied.
Shown in the table 5, methane is at 7.504 atmospheric pressure, below-130 ℃, and recovery just can be liquefied.
It is C that high-pressure and low-temperature condensing recovery method of the present invention can reclaim the charcoal number
2And C
2Above low boiling volatile organic steam, promptly can recovered oil gas in 98% hydrocarbons, control exhaust emissions concentration≤25g/m
3
The saturated liquid character of table 4 ethene
| Saturation pressure (gauge pressure kg/cm 2) | Saturation temperature (℃) |
| 0.01 | -103.77 |
| 0.56 | -96 |
| 1.13 | -90 |
| 2.11 | -82 |
| 7.68 | -56 |
| 10.48 | -50 |
Saturation pressure (the gauge pressure kg/cm of table 5 part material
2) and saturation temperature (℃) table of comparisons
| Saturation pressure | Saturation temperature | Saturation pressure | Saturation temperature | |
| Nitrogen | 4.581 | -180 | 9.387 | -170 |
| Oxygen | 6.612 | -160 | 11.98 | -150 |
| Methane | 7.504 | -130 | 11.93 | -120 |
| Ethene | 7.440 | -60 | 10.48 | -50 |
| Ethane | 7.748 | -40 | 10.605 | -30 |
| Propylene | 7.744 | 10 | 10.12 | 20 |
| Propane | 8.299 | 20 | 10.708 | 30 |
| Allene | 8.676 | 30 | 11.77 | 40 |
| The 1-butylene | 7.557 | 60 | 9.535 | 70 |
| Butane | 8.035 | 70 | 10.049 | 80 |
| Water | 0 | 100 | 8.0 | 175 |
| Pentane | 8.873 | 120 | 10.80 | 130 |
| Ethanol | 7.378 | 140 | 9.570 | 150 |
| Benzene | 8.501 | 170 | 10.18 | 160 |
| Heptane | 6.734 | 180 | 8.096 | 190 |
| Toluene | 8.873 | 210 | 10.48 | 220 |
| Ethylbenzene | 8.667 | 240 | 10.16 | 250 |
Under the state that the gasoline vapor retracting device moves continuously:
Liquid holdup in vapour storage tank 4 and the gas-liquid separator 5 can increase gradually, and needing in time derives; Liquid holdup in the Low Temperature Steam trap 7 can increase gradually, needs discharging in time; The liquefaction separating effect that can cause equipment that gathers of on-condensible gas reduces in the system.
Its solution is:
By opening explosion-proof solenoid valve V41A, hand-operated valve V41B, make the liquid that is trapped in vapour storage tank 4 and the gas-liquid separator 5, enter by the road in the oil storage tank 1 and reclaim.
By opening explosion-proof solenoid valve V71A, hand-operated valve V71B, make the liquid that is trapped in the Low Temperature Steam trap 7, enter in the oil storage tank 1 by pipeline with insulating.
By the opening pressure value of reasonable setting check valve V70C, can reduce the fixed gas scale of construction that accumulates in the Low Temperature Steam trap 7.When the temperature of setting the Low Temperature Steam trap is-95 ℃, when the pressure of organic steam is 0.15MPa, can all reclaim ethene steam.(referring to the listed data of table 5).
B on the vapour storage tank 4 is a rupture pressure disc.Vapour storage tank 4 has used HAN to intercept explosion-proof technology, when this can guarantee that gas compressor 2 inhaled concentrations are lower than 6% " air/vapor oil vapour ", can security incident not take place because of compression.
By the opening pressure of explosion-proof solenoid valve V57A, hand-operated valve V57B, check valve V57C and explosion-proof solenoid valve V71A, hand-operated valve V71B, check valve V71C rationally is set, can keep the pressure differential at Low Temperature Steam trap 7 two ends.
Explosion-proof electro connecting pressure gauge P2 control explosion-proof solenoid valve V57A; Explosion-proof electro connecting pressure gauge P3 control explosion-proof solenoid valve V71A.
Explosion-proof electro connecting pressure gauge P4 control explosion-proof solenoid valve V70A is in order to control (release) Low Temperature Steam trap 7 pressure inside.
During the work of gasoline vapor retracting device, hand-operated valve V12, V12B, V41B, V57B, V70B, V71B lead directly to.
When needing the recovering effect of analytical equipment, take gaseous sample from manual sampling valve VZ1, VZ2.
Among the present invention, Cryo Refrigerator 6 adopts classical " binary cascade refrigeration system ", preferable selection can be adopted " auto-cascading refrigeration system ", gas compressor 2 is the oil-free lubrication type, what Low Temperature Steam trap 7 used is plate-fin heat exchanger, and the heat transfer area density of plate-fin heat exchanger can reach 15000m
2/ m
3, refrigeration compressor has adopted a large amount of scroll compressors that use in general cool equipment.The liquid that discharges in the Low Temperature Steam trap 7 needs to enter oil storage tank 1 by utilidor.
A whole set of gasoline vapor retracting device can be arranged on the safety zone away from oil storage tank 1 (ground tank), increases the safety anti-explosive effect.
The present invention is owing to be increased to 0.85MPa with the pressure of gasoline vapor fluid, that is the saturation temperature when having improved this fluid liquefaction, therefore, can be under temperature conditions far above-110 ℃, reclaim that the charcoal number is C in the gasoline vapor
2And C
2Above low boiling point hydrocarbon makes tail gas reach the discharge standard of laws and regulations requirement.
Claims (4)
1. the high-pressure and low-temperature condensing recovery method of volatile organic steam in the oil gas, it is characterized in that: at first utilize gas compressor that the volatile organic steam that overflows in oil storage tank is aspirated supercharging, in aftercooler, make high boiling point organic compound liquefaction then, organic steam liquid after the liquefaction is discharged through the air accumulator bottom and is entered the oil storage tank recovery, organic steam after the liquefaction is behind gas separator, liquid is discharged through the separator bottom and is entered the oil storage tank recovery, discharge entered the oil storage tank recovery after steam entered and condensed into liquid in the Low Temperature Steam trap, and surplus is disposed in the atmosphere.
2. high-pressure and low-temperature condensing recovery method according to claim 1 is characterized in that: when the Low Temperature Steam trap was collected organic steam, operating temperature was not less than-95 ℃, operating pressure and is not higher than 1.0MPa.
3. high-pressure and low-temperature condensing recovery method according to claim 2 is characterized in that: when the Low Temperature Steam trap was collected organic steam, operating temperature was not less than-75 ℃, operating pressure and is not higher than 0.85MPa.
4. according to claim 2 or 3 described high-pressure and low-temperature condensing recovery methods, it is characterized in that: the vapor stream temperature of aftercooler outlet is not higher than 40 ℃.
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| CNA2008100330398A CN101306259A (en) | 2008-01-24 | 2008-01-24 | High-pressure and low-temperature condensing recovery method of volatile organic steam in oil gas |
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|---|---|---|---|
| CNA2008100330398A CN101306259A (en) | 2008-01-24 | 2008-01-24 | High-pressure and low-temperature condensing recovery method of volatile organic steam in oil gas |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103471246A (en) * | 2013-08-20 | 2013-12-25 | 宁夏宝塔石化科技实业发展有限公司 | Method for avoiding loss and damage by reducing heat carrier sudden boiling |
| CN105413390A (en) * | 2015-12-15 | 2016-03-23 | 安徽科海压缩机制造有限公司 | System for adsorption and pressure-boosting recovery of volatile organic compound steam in oil gas |
| CN106237647A (en) * | 2016-09-08 | 2016-12-21 | 南京中特化工动力设备有限公司 | Single variety volatile organic work material storage tank nitrogen circulation material recovery process |
| CN106697658A (en) * | 2016-12-21 | 2017-05-24 | 谢玉勋 | Control system for recycling safety of storage tank oil gas and control method thereof |
| CN112896833A (en) * | 2019-12-04 | 2021-06-04 | 中国石油化工股份有限公司 | Storage tank exhaust emission reduction system and method |
-
2008
- 2008-01-24 CN CNA2008100330398A patent/CN101306259A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103471246A (en) * | 2013-08-20 | 2013-12-25 | 宁夏宝塔石化科技实业发展有限公司 | Method for avoiding loss and damage by reducing heat carrier sudden boiling |
| CN105413390A (en) * | 2015-12-15 | 2016-03-23 | 安徽科海压缩机制造有限公司 | System for adsorption and pressure-boosting recovery of volatile organic compound steam in oil gas |
| CN105413390B (en) * | 2015-12-15 | 2018-05-25 | 安徽科海压缩机制造有限公司 | The absorption supercharging recovery system of volatile organic steam in a kind of oil gas |
| CN106237647A (en) * | 2016-09-08 | 2016-12-21 | 南京中特化工动力设备有限公司 | Single variety volatile organic work material storage tank nitrogen circulation material recovery process |
| CN106697658A (en) * | 2016-12-21 | 2017-05-24 | 谢玉勋 | Control system for recycling safety of storage tank oil gas and control method thereof |
| CN106697658B (en) * | 2016-12-21 | 2018-12-11 | 谢玉勋 | Gas of oil storage tank recycles safety control system and its control method |
| CN112896833A (en) * | 2019-12-04 | 2021-06-04 | 中国石油化工股份有限公司 | Storage tank exhaust emission reduction system and method |
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Application publication date: 20081119 |