CN105567288B - A kind of light hydrocarbon recovery system and method - Google Patents
A kind of light hydrocarbon recovery system and method Download PDFInfo
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- CN105567288B CN105567288B CN201510974117.4A CN201510974117A CN105567288B CN 105567288 B CN105567288 B CN 105567288B CN 201510974117 A CN201510974117 A CN 201510974117A CN 105567288 B CN105567288 B CN 105567288B
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 202
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 202
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 106
- 238000011084 recovery Methods 0.000 title claims abstract description 84
- 238000000034 method Methods 0.000 title claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 56
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 238000004064 recycling Methods 0.000 claims description 10
- 239000000498 cooling water Substances 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 238000009833 condensation Methods 0.000 abstract description 7
- 230000005494 condensation Effects 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 6
- 238000000926 separation method Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 59
- 239000012071 phase Substances 0.000 description 21
- 239000007789 gas Substances 0.000 description 19
- 239000000047 product Substances 0.000 description 17
- 239000007788 liquid Substances 0.000 description 9
- 230000001276 controlling effect Effects 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000005194 fractionation Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000003754 machining Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000002199 base oil Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 210000004209 hair Anatomy 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000006277 sulfonation reaction Methods 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/304—Pour point, cloud point, cold flow properties
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/14—White oil, eating oil
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of light hydrocarbon recovery systems, including：Lighter hydrocarbons recovery tower；Entrance exports the air cooler being connected with lighter hydrocarbons recovery column overhead, and the air cooler top is provided with temperature control executive device；Entrance exports the water cooler being connected with air cooler；Entrance exports the light hydrocarbon separator being connected with water cooler, and temperature control equipment is provided on the light hydrocarbon separator；The light ends unit that entrance is connected with light hydrocarbon separator gas vent.The initial gross separation that light hydrocarbon recovery system provided by the invention passes through lighter hydrocarbons recovery tower, the temperature control twice and condensation of air cooler and water cooler, it eventually arrives at light hydrocarbon separator and carries out lighter hydrocarbons separation, lighter hydrocarbons to be recycled and fine white oil, so that alleviating the load of fractionating column compared with the existing technology, it improves the recovery utilization rate of lighter hydrocarbons, reduce plant energy consumption, while improving the product quality of fine white oil.
Description
Technical field
The present invention relates to oil refinery technical fields, more particularly, to a kind of light hydrocarbon recovery system and method.
Background technology
Refined white oil is ultra-deep refined specialty minerals oil product, and component is usually the ring that molecular weight is 250~400
Alkane and alkane belong to lube cut, colourless, tasteless, odorless, have chemical inertness and excellent light, thermostability, purposes wide
It is general.White oil is paid attention to by domestic petroleum chemical industry as emerging product item.
Domestic production white oil mainly uses base oil sulfonation production at present, and cost is higher, and environmental pollution is larger, production
Quality is also unstable.With the development of oil hydrogenation technique technology, the sixties, foreign countries occurred producing the hydrofinishing of white oil
Technology.Have the characteristics that high income, three wastes generate, production is flexible, product quality is excellent etc..
Existing white oil hydrogenation plant is to utilize to be hydrocracked unconverted oil by secondary plus hydrogen production white oil product.Its
Product has the characteristics that good chemical inertness and excellent light, thermal stability and low temperature flow are strong.But existing technique
In, after hydrogen and feedstock oil react in the reactor, reaction product enters high-pressure separator, wherein gas phase after controlling temperature
Circulating hydrogen compressor is reached, liquid phase high score oil reaches low pressure separator, and low point of oil in low pressure separator passes through heat exchanger
Heating furnace is reached after heat exchange and further heats raising temperature, finally finally obtains product by vacuum fractionation tower.But above-mentioned work
In skill, further heated since low point of oil directly reaches heating furnace by heat exchanger heat exchange, into after vacuum fractionation tower, due to low
Divide the lighter hydrocarbons contained by oil more (about 2~6%), evaporating capacity is caused to increase, when especially low point of oil nature lightens, light component content
It is especially more, vacuum fractionation tower vacuum degree is seriously affected, if machining load can vacuumize load, raising when relatively low by improving
Regurgitant volume obtains qualified products, but when raising machining load, since the pressure of the higher fractionating column of evaporating capacity is higher, is unable to get conjunction
Lattice product cannot be satisfied normal process load.
Invention content
In view of this, the technical problem to be solved in the present invention is to increase lighter hydrocarbons recovery before low point of oil enters heating furnace
System, to improve the recovery utilization rate of lighter hydrocarbons.
The present invention provides a kind of light hydrocarbon recovery systems, including：
Lighter hydrocarbons recovery tower；
Entrance exports the air cooler being connected with lighter hydrocarbons recovery column overhead, and temperature control is provided on the air cooler and executes dress
It sets；
Entrance exports the water cooler being connected with air cooler；
Entrance exports the light hydrocarbon separator being connected with water cooler, and temperature control equipment is provided on the light hydrocarbon separator；
The light ends unit that entrance is connected with light hydrocarbon separator gas vent.
Preferably, the temperature control equipment on the light hydrocarbon separator is to be set to water cooler outlet with light hydrocarbon separator to enter
Threeway regulating device between mouthful.
Preferably, the threeway regulating device is connected with water cooler, air cooler and light hydrocarbon separator respectively.
Preferably, the light hydrocarbon separator oil phase outlet is connected to lighter hydrocarbons recovery column overhead by delivery pump.
The present invention provides a kind of method that the light hydrocarbon recovery system using described in above-mentioned technical proposal recycles lighter hydrocarbons, packets
It includes：
Low point of oil enters lighter hydrocarbons recovery tower, and by rectifying, gas phase portion is by tower top outlet by air cooler, water cooler two
Secondary condensation reaches light hydrocarbon separator, the lighter hydrocarbons that the gas phase at the top of light hydrocarbon separator is recycled by light ends unit；It is described
The outlet temperature of air cooler is 80~90 DEG C；The inlet temperature of the light hydrocarbon separator is 50~60 DEG C.
Preferably, low point of oily temperature is 270~300 DEG C after the heating.
Preferably, the water temperature of the water cooler cooling water inlet is 0~32 DEG C.
Preferably, the tower top temperature of the lighter hydrocarbons recovery tower is 160~180 DEG C.
Preferably, the tower top pressure of the lighter hydrocarbons recovery tower is 0.2~0.25Mpa.
Preferably, light hydrocarbon separator dehydration circle position is 45%~55%.
Compared with prior art, the present invention provides a kind of light hydrocarbon recovery systems, including：Lighter hydrocarbons recovery tower；Entrance with it is light
Hydrocarbon recovery tower tower top outlet connected air cooler is provided with temperature control executive device on the air cooler；Entrance and air cooler
The connected water cooler in outlet；Entrance exports the light hydrocarbon separator being connected with water cooler, and temperature is provided on the light hydrocarbon separator
Control device；The light ends unit that entrance is connected with light hydrocarbon separator gas vent.Light hydrocarbon recovery system provided by the invention
By the initial gross separation of lighter hydrocarbons recovery tower, the temperature control twice and condensation of air cooler and water cooler, eventually arrive at light hydrocarbon separator into
Row gas-liquid separation, the lighter hydrocarbons to be recycled and fine white oil, so that alleviating fractionating column compared with the existing technology
Load, improve the recovery utilization rate of lighter hydrocarbons, while improving the product quality of fine white oil.
Description of the drawings
Fig. 1 is light hydrocarbon recovery system particular flow sheet provided by the invention.
Specific implementation mode
The present invention provides a kind of light hydrocarbon recovery systems, including：
Lighter hydrocarbons recovery tower；
Entrance exports the air cooler being connected with lighter hydrocarbons recovery column overhead, and temperature control is provided on the air cooler and executes dress
It sets；
Entrance exports the water cooler being connected with air cooler；
Entrance exports the light hydrocarbon separator being connected with water cooler, and temperature control equipment is provided on the light hydrocarbon separator；
The light ends unit that entrance is connected with light hydrocarbon separator gas vent.
Light hydrocarbon recovery system provided by the invention includes lighter hydrocarbons recovery tower, and the present invention is to the lighter hydrocarbons recovery tower without limit
It is fixed, rectifying column well known to those skilled in the art.
In the present invention, the tower top temperature of the lighter hydrocarbons recovery tower is preferably 160~180 DEG C, more preferably 165~175
℃；Pressure is preferably 0.2~0.25Mpa.
In the present invention, low point of oil enters lighter hydrocarbons recovery tower, and the low point of oily temperature is preferably 270~300 DEG C.
The present invention can be more by controlling the tower top temperature, pressure and the temperature of low point of oil entrance of above-mentioned lighter hydrocarbons recovery tower
Rectifying in good control lighter hydrocarbons recovery tower, to preferably improve product quality.
Light hydrocarbon recovery system provided by the invention includes that entrance exports the air cooler being connected with lighter hydrocarbons recovery column overhead, described
Temperature control executive device is provided on air cooler.
The present invention for above-mentioned air cooler model and specification without limit, air cooler well known to those skilled in the art
.
Air cooler of the present invention is preferably the air cooler with executing agency；Temperature for automatically controlling air cooler, institute
It is 80~90 DEG C to state air cooler outlet temperature.
It is tentatively condensed under above-mentioned specific temperature from the lighter hydrocarbons of lighter hydrocarbons recovery tower gas vent by air cooler, then
Reach water cooler.
Light hydrocarbon recovery system provided by the invention includes that entrance exports the water cooler being connected with air cooler.
The present invention for above-mentioned water cooler model and specification without limit, water cooler well known to those skilled in the art
.
In the present invention, the temperature of the cooling water inlet of the water cooler is 0~32 DEG C, more preferably 25~30 DEG C.
The present invention can preferably carry out condensation to product quality by the control of the temperature of above-mentioned air cooler and water cooler
It further increases, the rate of recovery of stable light hydrocarbon.
Light hydrocarbon recovery system provided by the invention includes that entrance exports the light hydrocarbon separator being connected, the lighter hydrocarbons with water cooler
Temperature control equipment is provided on separator.
In the present invention, the temperature control equipment can be to be set between water cooler outlet and light hydrocarbon separator entrance
Threeway regulating device.Preferably, the threeway regulating device is connected with water cooler, air cooler and light hydrocarbon separator respectively, leads to
It crosses air cooler and water cooler and adjusts light hydrocarbon separator temperature jointly.The outlet of wherein water cooler is served as theme, and the outlet of air cooler is
By-pass adjusts light hydrocarbon separator temperature by temperature difference jointly.Preferably, control gas-liquid separator temperature is 50~60 DEG C.
The present invention for above-mentioned light hydrocarbon separator and threeway regulating device model and specification without limit, this field skill
Light hydrocarbon separator and threeway regulating device known to art personnel.
The gas vent of light hydrocarbon separator of the present invention is connected with light ends unit；The oil phase of gas-liquid separator exports
Water phase for fine white oil, gas-liquid separator exports, can be down to treatment center of sewage by being dehydrated regulating valve.
Light hydrocarbon separator dehydration packet circle position preferably 45%~55% of the present invention.
Water-oil separating can be carried out well by controlling above-mentioned dehydration circle position.
In the present invention, the light hydrocarbon separator oil phase outlet is connected to lighter hydrocarbons recovery column overhead by delivery pump.
Some fine white oil is namely back to lighter hydrocarbons recovery column overhead by delivery pump.Overhead reflux contributes to more preferably
The temperature and pressure of ground stable light hydrocarbon recovery tower ensures lighter hydrocarbons quality and fine white oil product quality.
Light hydrocarbon recovery system provided by the invention includes the lighter hydrocarbons recovery dress that entrance is connected with light hydrocarbon separator gas vent
It sets, the lighter hydrocarbons being recycled.
In the present invention, the light ends unit can be recycled directly or directly be utilized.The light ends unit can
Think lighter hydrocarbons storage tank, lighter hydrocarbons are directly recycled.The light ends unit can be delivered to fuel gas by lighter hydrocarbons supercharger
Pipe network so that lighter hydrocarbons directly utilize.
Lighter hydrocarbons supercharger pressure can be configured according to the pressure needed for fuel gas pipe network, so that the lighter hydrocarbons of recycling
It can preferably be utilized.
As shown in FIG. 1, FIG. 1 is this hairs for the one of technical solution particular flow sheet of light hydrocarbon recovery system provided by the invention
The light hydrocarbon recovery system particular flow sheet of bright offer, specifically：
1 is low point of oil；2 be bottom of tower oil；3 be lighter hydrocarbons recovery tower；4 be air cooler；5 be water cooler；6 be cooling water inlet；7
For cooling water outlet；8 be light hydrocarbon separator；9 be threeway regulating device；10 be lighter hydrocarbons supercharger；11 be delivery pump；12 be lighter hydrocarbons
Separator water phase exports；13 export for light hydrocarbon separator oil phase.
The present invention provides a kind of method that the light hydrocarbon recovery system using described in above-mentioned technical proposal recycles lighter hydrocarbons, packets
It includes：
Low point of oil enters lighter hydrocarbons recovery tower, and by rectifying, gas phase portion is by tower top outlet by air cooler, water cooler two
Secondary condensation reaches light hydrocarbon separator, the lighter hydrocarbons that the gas phase of light hydrocarbon separator is recycled by light ends unit；It is described air-cooled
The outlet temperature of device is 80~90 DEG C；The inlet temperature of the gas-liquid separator is 50~60 DEG C.
Methods of light hydrocarbon recovery of the present invention is that the low point of oil separated by low pressure separator is carried through heat exchange first
After temperature top gaseous phase part and bottom of tower liquid phase oil product are obtained by rectifying into lighter hydrocarbons recovery tower.
Wherein bottom of tower oil product is fed directly to fractionating system, i.e., conventional vacuum fractionation tower carries out subsequent step.
In the present invention, the tower top temperature of the lighter hydrocarbons recovery tower is preferably 160~180 DEG C, more preferably 165~175
℃；Tower top pressure is preferably 0.2~0.25Mpa.
In the present invention, low point of oil enters lighter hydrocarbons recovery tower, and the low point of oily temperature is preferably 270~300 DEG C.
Wherein gas phase portion is condensed by tower top outlet by air cooler, water cooler and reaches light hydrocarbon separator, lighter hydrocarbons twice
The lighter hydrocarbons that the gas phase lighter hydrocarbons of separator are recycled by light ends unit, the outlet of light hydrocarbon separator oil phase are fine white oil.
The present invention for above-mentioned air cooler model and specification without limit, air cooler well known to those skilled in the art
.
Air cooler of the present invention is preferably the air cooler with executing agency；Temperature for automatically controlling air cooler, institute
It is 80~90 DEG C to state air cooler outlet temperature.
The present invention for above-mentioned water cooler model and specification without limit, water cooler well known to those skilled in the art
.
In the present invention, the temperature of the cooling water inlet of the water cooler is 0~32 DEG C, more preferably 25~30 DEG C.
The present invention can preferably carry out condensation to product quality by the control of the temperature of above-mentioned air cooler and water cooler
It further increases, the rate of recovery of stable light hydrocarbon.
Temperature control executive device is provided on the light hydrocarbon separator, control light hydrocarbon separator inlet temperature is 50~60
℃；The light hydrocarbon separator oil phase outlet is fine white oil.
In the present invention, the temperature control equipment can be to be set between water cooler outlet and light hydrocarbon separator entrance
Threeway regulating device.Preferably, the threeway regulating device is connected with water cooler, air cooler and light hydrocarbon separator respectively, leads to
It crosses air cooler and water cooler and adjusts light hydrocarbon separator inlet temperature jointly.The outlet of wherein water cooler is served as theme, and air cooler goes out
Mouth is by-pass, adjusts light hydrocarbon separator inlet temperature jointly by temperature difference.Preferably, control light hydrocarbon separator inlet temperature is
50~60 DEG C.
Light hydrocarbon separator dehydration packet circle position preferably 45%~55% of the present invention.
Water-oil separating can be carried out well by controlling above-mentioned dehydration circle position.
In the present invention, the light hydrocarbon separator oil phase outlet is connected to lighter hydrocarbons recovery column overhead by delivery pump.
Some fine white oil is namely back to lighter hydrocarbons recovery column overhead by delivery pump.Overhead reflux contributes to more preferably
The temperature and pressure of ground stable light hydrocarbon recovery tower ensures lighter hydrocarbons quality and fine white oil product quality.
In the present invention, the light ends unit can be recycled directly or directly be utilized.The light ends unit can
Think lighter hydrocarbons storage tank, lighter hydrocarbons are directly recycled.The light ends unit can be delivered to fuel gas by lighter hydrocarbons supercharger
Pipe network so that lighter hydrocarbons directly utilize.
Lighter hydrocarbons supercharger pressure can be configured according to the pressure needed for fuel gas pipe network, so that the lighter hydrocarbons of recycling
It can preferably be utilized.
The present invention provides a kind of light hydrocarbon recovery systems, including：Lighter hydrocarbons recovery tower；Entrance is exported with lighter hydrocarbons recovery column overhead
Connected air cooler is provided with temperature control executive device on the air cooler；Entrance exports the water cooler being connected with air cooler；
Entrance exports the light hydrocarbon separator being connected with water cooler, and temperature control equipment is provided on the light hydrocarbon separator；Entrance with it is light
The connected light ends unit in hydrocarbon separator gas outlet.Light hydrocarbon recovery system provided by the invention passes through the first of lighter hydrocarbons recovery tower
Step separation, the temperature control twice and condensation of air cooler and water cooler eventually arrive at light hydrocarbon separator and carry out gas-liquid separation, to obtain
The lighter hydrocarbons of recycling and fine white oil improve returning for lighter hydrocarbons so that alleviating the load of fractionating column compared with the existing technology
Utilization rate is received, while improving the product quality of fine white oil.
In order to further illustrate the present invention, with reference to embodiments to light hydrocarbon recovery system provided by the invention and method into
Row detailed description.
Embodiment 1
Light hydrocarbon recovery system is prepared, specially：Board-like single overflow lighter hydrocarbons recovery tower and board-like single overflow lighter hydrocarbons recovery tower tower
The connected variable angle adjustable type air cooler of mouth is ejected, the U-tube shell-type water cooler being connected is exported with variable angle adjustable type air cooler；
Entrance exports the horizontal light hydrocarbon separator being connected with U-tube shell-type water cooler；Entrance and horizontal light hydrocarbon separator gas vent phase
Lighter hydrocarbons are delivered to fuel gas pipe network by reciprocating lighter hydrocarbons supercharger even, reciprocating supercharger.
Embodiment 2
Above-mentioned light hydrocarbon recovery system is used in the hydroisomerizing system of white oil, low point of oil enters controlled at 270 DEG C
Low point of oil mass of lighter hydrocarbons recovery tower is 24t/h, and lighter hydrocarbons recovery column overhead temperatures are 160 DEG C, pressure 0.2Mpa, by rectifying, gas
Mutually part is condensed by tower top outlet by air cooler, water cooler and reaches light hydrocarbon separator twice, and air cooler temperature is 85 DEG C；Water
Cooler cooling water is 20 DEG C；Gas-liquid separator inlet temperature is 50 DEG C；It is 50% to be dehydrated boundary position, and the gas phase of light hydrocarbon separator passes through
The lighter hydrocarbons that light ends unit is recycled, the outlet of light hydrocarbon separator oil phase are fine white oil.It is computed, the lighter hydrocarbons amount of recycling is
100NM3The fine white oil amount of/h, generation are 1.1t/h.
Embodiment 3
Above-mentioned light hydrocarbon recovery system is used in the hydroisomerizing system of white oil, low point of oil enters controlled at 280 DEG C
Low point of oil mass of lighter hydrocarbons recovery tower is 24t/h, and lighter hydrocarbons recovery column overhead temperatures are 170 DEG C, pressure 0.25Mpa, by rectifying, gas
Mutually part is condensed by tower top outlet by air cooler, water cooler and reaches gas-liquid separator twice, and air cooler temperature is 90 DEG C；Water
Cooler cooling water is 20 DEG C；Gas-liquid separator inlet temperature is 60 DEG C；It is 50% to be dehydrated boundary position, and the gas phase of light hydrocarbon separator passes through
The lighter hydrocarbons that light ends unit is recycled, the outlet of light hydrocarbon separator oil phase are fine white oil.It is computed, the lighter hydrocarbons amount of recycling is
240NM3The fine white oil amount of/h, generation are 1.5t/h.
The above is only a preferred embodiment of the present invention, it is noted that for the ordinary skill people of the art
For member, various improvements and modifications may be made without departing from the principle of the present invention, these improvements and modifications are also answered
It is considered as protection scope of the present invention.
Claims (8)
1. a kind of light hydrocarbon recovery system of white oil, including：
Lighter hydrocarbons recovery tower；
Entrance exports the air cooler being connected with lighter hydrocarbons recovery column overhead, and the air cooler top is provided with temperature control and executes dress
It sets；
Entrance exports the water cooler being connected with air cooler；
Entrance exports the light hydrocarbon separator being connected with water cooler, and temperature control equipment is provided on the light hydrocarbon separator；It is described
Temperature control equipment on light hydrocarbon separator is that the threeway being set between water cooler outlet and light hydrocarbon separator entrance adjusts dress
It sets；The threeway regulating device is connected with water cooler, air cooler and light hydrocarbon separator respectively；The outlet of water cooler is served as theme, empty
The outlet of cooler is by-pass, adjusts light hydrocarbon separator temperature jointly by temperature difference；
The light ends unit that entrance is connected with light hydrocarbon separator gas vent.
2. light hydrocarbon recovery system according to claim 1, which is characterized in that the light hydrocarbon separator oil phase outlet passes through defeated
Pump is sent to be connected to lighter hydrocarbons recovery column overhead.
3. a kind of method that lighter hydrocarbons are recycled using light hydrocarbon recovery system described in claim 1, including：
Low point of oil enters lighter hydrocarbons recovery tower, and by rectifying, gas phase portion is cold twice by air cooler, water cooler by tower top outlet
Lighter hydrocarbons solidifying to reach light hydrocarbon separator, that the gas phase lighter hydrocarbons of light hydrocarbon separator are recycled by light ends unit；It is described air-cooled
The outlet temperature of device is 80~90 DEG C；The inlet temperature of the light hydrocarbon separator is 50~60 DEG C.
4. the method for recycling lighter hydrocarbons according to claim 3, which is characterized in that the low point of oily temperature is 270~300
℃。
5. the method for recycling lighter hydrocarbons according to claim 3, which is characterized in that the water temperature of the water cooler cooling water inlet
It is 0~32 DEG C.
6. the method for recycling lighter hydrocarbons according to claim 3, which is characterized in that the tower top temperature of the lighter hydrocarbons recovery tower is
160~180 DEG C.
7. the method for recycling lighter hydrocarbons according to claim 3, which is characterized in that the tower top pressure of the lighter hydrocarbons recovery tower is
0.2~0.25Mpa.
8. the method for recycling lighter hydrocarbons according to claim 3, which is characterized in that light hydrocarbon separator dehydration circle position is
45%~55%.
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| CN201510974117.4A CN105567288B (en) | 2015-12-17 | 2015-12-17 | A kind of light hydrocarbon recovery system and method |
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|---|---|---|---|---|
| CN201678635U (en) * | 2010-03-18 | 2010-12-22 | 中国石油化工集团公司 | Light-hydrocarbon recycling device |
| CN103361105A (en) * | 2012-04-05 | 2013-10-23 | 中国石油天然气股份有限公司 | Simple separation method for separating catalytically cracked gasoline into light gasoline and heavy gasoline |
| CN204356288U (en) * | 2014-12-05 | 2015-05-27 | 四川中腾能源科技有限公司 | A kind of weight hydrocarbon separation system |
| CN105062545B (en) * | 2015-08-21 | 2016-08-17 | 中石化宁波工程有限公司 | A kind of methods of light hydrocarbon recovery |
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2015
- 2015-12-17 CN CN201510974117.4A patent/CN105567288B/en active Active
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