CN105567288A - Light hydrocarbon recycling system and method - Google Patents
Light hydrocarbon recycling system and method Download PDFInfo
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- CN105567288A CN105567288A CN201510974117.4A CN201510974117A CN105567288A CN 105567288 A CN105567288 A CN 105567288A CN 201510974117 A CN201510974117 A CN 201510974117A CN 105567288 A CN105567288 A CN 105567288A
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- light hydrocarbon
- lighter hydrocarbons
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 206
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 206
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 120
- 238000000034 method Methods 0.000 title claims description 22
- 238000004064 recycling Methods 0.000 title abstract 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 57
- 238000009833 condensation Methods 0.000 claims abstract description 12
- 230000005494 condensation Effects 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims description 86
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 239000000498 cooling water Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 55
- 239000012071 phase Substances 0.000 description 20
- 239000000047 product Substances 0.000 description 17
- 239000007789 gas Substances 0.000 description 11
- 239000007788 liquid Substances 0.000 description 9
- 239000002737 fuel gas Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000003754 machining Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000010687 lubricating oil Substances 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
- 238000000746 purification Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance 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 invention provides a light hydrocarbon recycling system which comprises a light hydrocarbon recycling tower, an air cooler, a water cooler, a light hydrocarbon separator and a light hydrocarbon recycling device. An inlet of the air cooler is connected with an outlet at the top of the light hydrocarbon recycling tower, a temperature control executing device is arranged on the upper portion of the air cooler, an inlet of the water cooler is connected with an outlet of the air cooler, an inlet of the light hydrocarbon separator is connected with an outlet of the water cooler, a temperature control device is arranged on the light hydrocarbon separator, and an inlet of the light hydrocarbon recycling device is connected with a gas outlet of the light hydrocarbon separator. Light hydrocarbon is preliminarily separated through the light hydrocarbon recycling tower and subjected to temperature control and condensation for two times and finally reaches the light hydrocarbon separator for further separation to obtain recycled light hydrocarbon and fine white oil, so that compared with the prior art, the light hydrocarbon recycling system has the advantages that load of a distilling tower is reduced, recycling rate of light hydrocarbon is increased, device energy consumption is lowered, and product quality of the fine white oil is improved.
Description
Technical field
The present invention relates to oil purification technical field, especially relate to a kind of light hydrocarbon recovery system and method.
Background technology
It is ultra-deep refining specialty minerals oil prod that white oil is refined, its component to be generally molecular weight be 250 ~ 400 naphthenic hydrocarbon and alkane, belong to lubricating oil distillate, colourless, tasteless, odorless, there is unreactiveness and excellent light, heat-resistant quality, of many uses.White oil, as emerging product item, is being subject to the attention of domestic petroleum chemical industry.
Current domestic production white oil mainly adopts base oil sulfonation production, and its cost is higher, and environmental pollution is comparatively large, and quality product is also unstable.Along with the development of oil hydrogenation technique technology, there is the hydrofining technology technology of producing white oil the sixties abroad.Have yield high, produce without the three wastes, produce flexibly, the excellent feature of quality product.
Existing white oil hydrogenation unit utilizes hydrocracking unconverted oil to produce white oil product through secondary hydrogenation.Its product has good unreactiveness and the feature such as excellent light, thermostability and low-temperature fluidity be strong.But in existing technique, after hydrogen and stock oil react in the reactor, reaction product enters high-pressure separator after control temperature, wherein gas phase arrives circulating hydrogen compressor, liquid phase high score oil arrives light pressure separator, and low point of oil in light pressure separator arrives process furnace after interchanger heat exchange heats raising temperature further, eventually pass vacuum fractionation tower and finally obtain product.But in above-mentioned technique, heat further because low point of oil directly arrives process furnace through interchanger heat exchange, after entering vacuum fractionation tower, lighter hydrocarbons more (about 2 ~ 6%) contained by low point of oil, evaporating capacity is caused to increase, when particularly low point of oil nature lightens, light constituent content is many especially, have a strong impact on vacuum fractionation tower vacuum tightness, if load can be vacuumized by raising when machining load is lower, improve quantity of reflux and obtain qualified product, but when improving machining load, because the pressure of the higher separation column of evaporating capacity is higher, qualified product cannot be obtained, normal process load cannot be met.
Summary of the invention
In view of this, the technical problem to be solved in the present invention is to increase light hydrocarbon recovery system before low point of oil enters process furnace, thus improves the recovery utilization rate of lighter hydrocarbons.
The invention provides a kind of light hydrocarbon recovery system, comprising:
Lighter hydrocarbons recovery tower;
Entrance exports with lighter hydrocarbons recovery column overhead the air cooler be connected, and described air cooler is provided with temperature and controls executive device;
Entrance exports with air cooler the water cooler be connected;
Entrance exports with water cooler the light hydrocarbon separator be connected, and described light hydrocarbon separator is provided with temperature-control device;
The light ends unit that entrance is connected with light hydrocarbon separator pneumatic outlet.
Preferably, the temperature-control device on described light hydrocarbon separator is be arranged at the threeway setting device between water cooler outlet and light hydrocarbon separator entrance.
Preferably, described threeway setting device is connected with light hydrocarbon separator with water cooler, air cooler respectively.
Preferably, described light hydrocarbon separator oil phase outlet is connected to lighter hydrocarbons recovery column overhead by transferpump.
The invention provides a kind of method adopting the light hydrocarbon recovery system described in technique scheme to reclaim lighter hydrocarbons, comprising:
Low point of oil enters lighter hydrocarbons recovery tower, and through rectifying, gas phase portion arrives light hydrocarbon separator by tower top outlet through air cooler, water cooler twice condensation, the lighter hydrocarbons that the gas phase at light hydrocarbon separator top is recycled by light ends unit; The temperature out of described air cooler is 80 ~ 90 DEG C; The temperature in of described light hydrocarbon separator is 50 ~ 60 DEG C.
Preferably, after described heating, low point of oily temperature is 270 ~ 300 DEG C.
Preferably, the water temperature of described water cooler cooling water inlet is 0 ~ 32 DEG C.
Preferably, the tower top temperature of described lighter hydrocarbons recovery tower is 160 ~ 180 DEG C.
Preferably, the tower top pressure of described lighter hydrocarbons recovery tower is 0.2 ~ 0.25Mpa.
Preferably, described light hydrocarbon separator dehydration position, circle is 45% ~ 55%.
Compared with prior art, the invention provides a kind of light hydrocarbon recovery system, comprising: lighter hydrocarbons recovery tower; Entrance exports with lighter hydrocarbons recovery column overhead the air cooler be connected, and described air cooler is provided with temperature and controls executive device; Entrance exports with air cooler the water cooler be connected; Entrance exports with water cooler the light hydrocarbon separator be connected, and described light hydrocarbon separator is provided with temperature-control device; The light ends unit that entrance is connected with light hydrocarbon separator pneumatic outlet.Light hydrocarbon recovery system provided by the invention is by the initial gross separation of lighter hydrocarbons recovery tower, twice temperature control of air cooler and water cooler and condensation, final arrival light hydrocarbon separator carries out gas-liquid separation, thus the lighter hydrocarbons be recycled and meticulous white oil, thus make the load alleviating separation column relative to prior art, improve the recovery utilization rate of lighter hydrocarbons, improve the quality product of meticulous white oil simultaneously.
Accompanying drawing explanation
Fig. 1 is light hydrocarbon recovery system particular flow sheet provided by the invention.
Embodiment
The invention provides a kind of light hydrocarbon recovery system, comprising:
Lighter hydrocarbons recovery tower;
Entrance exports with lighter hydrocarbons recovery column overhead the air cooler be connected, and described air cooler is provided with temperature and controls executive device;
Entrance exports with air cooler the water cooler be connected;
Entrance exports with water cooler the light hydrocarbon separator be connected, and described light hydrocarbon separator is provided with temperature-control device;
The light ends unit that entrance is connected with light hydrocarbon separator pneumatic outlet.
Light hydrocarbon recovery system provided by the invention comprises lighter hydrocarbons recovery tower, and the present invention does not limit described lighter hydrocarbons recovery tower, rectifying tower well known to those skilled in the art.
In the present invention, the tower top temperature of described lighter hydrocarbons recovery tower is preferably 160 ~ 180 DEG C, is more preferably 165 ~ 175 DEG C; Pressure is preferably 0.2 ~ 0.25Mpa.
In the present invention, low point of oil enters lighter hydrocarbons recovery tower, and described low point of oily temperature is preferably 270 ~ 300 DEG C.
The present invention can better control rectifying in lighter hydrocarbons recovery tower by the temperature controlling the tower top temperature of above-mentioned lighter hydrocarbons recovery tower, pressure and low point of oil and enter, thus better improves the quality of products.
Light hydrocarbon recovery system provided by the invention comprises entrance and exports with lighter hydrocarbons recovery column overhead the air cooler be connected, and described air cooler is provided with temperature and controls executive device.
The present invention does not limit for the model of above-mentioned air cooler and specification, air cooler well known to those skilled in the art.
Air cooler of the present invention is preferably the air cooler of band topworks; For automatically controlling the temperature of air cooler, described air cooler temperature out is 80 ~ 90 DEG C.
Under above-mentioned specified temp, carry out preliminary condensation through air cooler from the lighter hydrocarbons of lighter hydrocarbons recovery tower pneumatic outlet, then arrive water cooler.
Light hydrocarbon recovery system provided by the invention comprises entrance and exports with air cooler the water cooler be connected.
The present invention does not limit for the model of above-mentioned water cooler and specification, water cooler well known to those skilled in the art.
In the present invention, the temperature of the cooling water inlet of described water cooler is 0 ~ 32 DEG C, is more preferably 25 ~ 30 DEG C.
The present invention controls to carry out condensation better by the temperature of above-mentioned air cooler and water cooler thus quality product improves further, the rate of recovery of stable light hydrocarbon.
Light hydrocarbon recovery system provided by the invention comprises entrance and exports with water cooler the light hydrocarbon separator be connected, and described light hydrocarbon separator is provided with temperature-control device.
In the present invention, described temperature-control device can for being arranged at the threeway setting device between water cooler outlet and light hydrocarbon separator entrance.Preferably, described threeway setting device is connected with light hydrocarbon separator with water cooler, air cooler respectively, jointly regulates light hydrocarbon separator temperature by air cooler and water cooler.Wherein the outlet of water cooler is served as theme, and the outlet of air cooler is by-pass, jointly regulates light hydrocarbon separator temperature by temperature head.Preferably, controlling gas-liquid separation actuator temperature is 50 ~ 60 DEG C.
The present invention does not limit for the model of above-mentioned light hydrocarbon separator and threeway setting device and specification, light hydrocarbon separator well known to those skilled in the art and threeway setting device.
The pneumatic outlet of light hydrocarbon separator of the present invention is connected with light ends unit; The oil phase outlet of gas-liquid separator is meticulous white oil, and the aqueous phase outlet of gas-liquid separator, can down to treatment center of sewage through dehydration variable valve.
Light hydrocarbon separator dehydration bag position, circle of the present invention is preferably 45% ~ 55%.
Oily water separation can be carried out well by controlling above-mentioned dehydration circle position.
In the present invention, described light hydrocarbon separator oil phase outlet is connected to lighter hydrocarbons recovery column overhead by transferpump.
Namely some fine white oil is back to lighter hydrocarbons recovery column overhead by transferpump.Trim the top of column contributes to the temperature and pressure of stable light hydrocarbon recovery tower better, ensures lighter hydrocarbons quality and meticulous white oil quality product.
Light hydrocarbon recovery system provided by the invention comprises the light ends unit that entrance is connected with light hydrocarbon separator pneumatic outlet, the lighter hydrocarbons be recycled.
In the present invention, described light ends unit can directly reclaim or directly utilize.Described light ends unit can be lighter hydrocarbons storage tank, is directly reclaimed by lighter hydrocarbons.Described light ends unit can be delivered to fuel gas pipe network by lighter hydrocarbons supercharger, and lighter hydrocarbons are directly utilized.
Lighter hydrocarbons supercharger pressure can be arranged by the pressure needed for based on fuel gas pipe network, thus the lighter hydrocarbons reclaimed can be utilized better.
As shown in Figure 1, Fig. 1 is light hydrocarbon recovery system particular flow sheet provided by the invention to one of them technical scheme particular flow sheet of light hydrocarbon recovery system provided by the invention, concrete:
1 is low point of oil; 2 is oil at the bottom of tower; 3 is lighter hydrocarbons recovery tower; 4 is air cooler; 5 is water cooler; 6 is cooling water inlet; 7 is cooling water outlet; 8 is light hydrocarbon separator; 9 is threeway setting device; 10 is lighter hydrocarbons supercharger; 11 is transferpump; 12 is the outlet of light hydrocarbon separator aqueous phase; 13 is the outlet of light hydrocarbon separator oil phase.
The invention provides a kind of method adopting the light hydrocarbon recovery system described in technique scheme to reclaim lighter hydrocarbons, comprising:
Low point of oil enters lighter hydrocarbons recovery tower, and through rectifying, gas phase portion arrives light hydrocarbon separator by tower top outlet through air cooler, water cooler twice condensation, the lighter hydrocarbons that the gas phase of light hydrocarbon separator is recycled by light ends unit; The temperature out of described air cooler is 80 ~ 90 DEG C; The temperature in of described gas-liquid separator is 50 ~ 60 DEG C.
First methods of light hydrocarbon recovery of the present invention enters lighter hydrocarbons recovery tower for the low point of oil separated through light pressure separator after heat exchange temperature raising, through rectifying, obtains liquid phase oil product at the bottom of top gaseous phase part and tower.
Wherein at the bottom of tower, oil product directly delivers to fractionating system, and namely conventional vacuum fractionation tower carries out subsequent step.
In the present invention, the tower top temperature of described lighter hydrocarbons recovery tower is preferably 160 ~ 180 DEG C, is more preferably 165 ~ 175 DEG C; Tower top pressure is preferably 0.2 ~ 0.25Mpa.
In the present invention, low point of oil enters lighter hydrocarbons recovery tower, and described low point of oily temperature is preferably 270 ~ 300 DEG C.
Wherein gas phase portion arrives light hydrocarbon separator by tower top outlet through air cooler, water cooler twice condensation, the lighter hydrocarbons that the gas phase lighter hydrocarbons of light hydrocarbon separator are recycled by light ends unit, and the outlet of light hydrocarbon separator oil phase is meticulous white oil.
The present invention does not limit for the model of above-mentioned air cooler and specification, air cooler well known to those skilled in the art.
Air cooler of the present invention is preferably the air cooler of band topworks; For automatically controlling the temperature of air cooler, described air cooler temperature out is 80 ~ 90 DEG C.
The present invention does not limit for the model of above-mentioned water cooler and specification, water cooler well known to those skilled in the art.
In the present invention, the temperature of the cooling water inlet of described water cooler is 0 ~ 32 DEG C, is more preferably 25 ~ 30 DEG C.
The present invention controls to carry out condensation better by the temperature of above-mentioned air cooler and water cooler thus quality product improves further, the rate of recovery of stable light hydrocarbon.
Described light hydrocarbon separator is provided with temperature and controls executive device, controlling light hydrocarbon separator temperature in is 50 ~ 60 DEG C; Described light hydrocarbon separator oil phase outlet is meticulous white oil.
In the present invention, described temperature-control device can for being arranged at the threeway setting device between water cooler outlet and light hydrocarbon separator entrance.Preferably, described threeway setting device is connected with light hydrocarbon separator with water cooler, air cooler respectively, jointly regulates light hydrocarbon separator temperature in by air cooler and water cooler.Wherein the outlet of water cooler is served as theme, and the outlet of air cooler is by-pass, jointly regulates light hydrocarbon separator temperature in by temperature head.Preferably, controlling light hydrocarbon separator temperature in is 50 ~ 60 DEG C.
Light hydrocarbon separator dehydration bag position, circle of the present invention is preferably 45% ~ 55%.
Oily water separation can be carried out well by controlling above-mentioned dehydration circle position.
In the present invention, described light hydrocarbon separator oil phase outlet is connected to lighter hydrocarbons recovery column overhead by transferpump.
Namely some fine white oil is back to lighter hydrocarbons recovery column overhead by transferpump.Trim the top of column contributes to the temperature and pressure of stable light hydrocarbon recovery tower better, ensures lighter hydrocarbons quality and meticulous white oil quality product.
In the present invention, described light ends unit can directly reclaim or directly utilize.Described light ends unit can be lighter hydrocarbons storage tank, is directly reclaimed by lighter hydrocarbons.Described light ends unit can be delivered to fuel gas pipe network by lighter hydrocarbons supercharger, and lighter hydrocarbons are directly utilized.
Lighter hydrocarbons supercharger pressure can be arranged by the pressure needed for based on fuel gas pipe network, thus the lighter hydrocarbons reclaimed can be utilized better.
The invention provides a kind of light hydrocarbon recovery system, comprising: lighter hydrocarbons recovery tower; Entrance exports with lighter hydrocarbons recovery column overhead the air cooler be connected, and described air cooler is provided with temperature and controls executive device; Entrance exports with air cooler the water cooler be connected; Entrance exports with water cooler the light hydrocarbon separator be connected, and described light hydrocarbon separator is provided with temperature-control device; The light ends unit that entrance is connected with light hydrocarbon separator pneumatic outlet.Light hydrocarbon recovery system provided by the invention is by the initial gross separation of lighter hydrocarbons recovery tower, twice temperature control of air cooler and water cooler and condensation, final arrival light hydrocarbon separator carries out gas-liquid separation, thus the lighter hydrocarbons be recycled and meticulous white oil, thus make the load alleviating separation column relative to prior art, improve the recovery utilization rate of lighter hydrocarbons, improve the quality product of meticulous white oil simultaneously.
In order to further illustrate the present invention, below in conjunction with embodiment, light hydrocarbon recovery system provided by the invention and method are described in detail.
Embodiment 1
Prepare light hydrocarbon recovery system, be specially: board-like single overflow lighter hydrocarbons recovery tower, export with board-like single overflow lighter hydrocarbons recovery column overhead the variable angle adjustable type air cooler be connected, export with variable angle adjustable type air cooler the U-tube shell-type water cooler be connected; Entrance exports with U-tube shell-type water cooler the horizontal light hydrocarbon separator be connected; The reciprocating lighter hydrocarbons supercharger that entrance is connected with horizontal light hydrocarbon separator pneumatic outlet, lighter hydrocarbons are delivered to fuel gas pipe network by reciprocating supercharger.
Embodiment 2
Above-mentioned light hydrocarbon recovery system is used in the hydroisomerizing system of white oil, low point of oily control temperature is 270 DEG C, entering lighter hydrocarbons recovery tower low point of oil mass is 24t/h, lighter hydrocarbons recovery column overhead temperatures is 160 DEG C, pressure is 0.2Mpa, through rectifying, gas phase portion arrives light hydrocarbon separator by tower top outlet through air cooler, water cooler twice condensation, and air cooler temperature is 85 DEG C; Water cooler water coolant is 20 DEG C; Gas-liquid separator temperature in is 50 DEG C; Dehydration position, circle is 50%, the lighter hydrocarbons that the gas phase of light hydrocarbon separator is recycled by light ends unit, and the outlet of light hydrocarbon separator oil phase is meticulous white oil.As calculated, the lighter hydrocarbons amount of recovery is 100NM
3/ h, the meticulous white oil amount of generation is 1.1t/h.
Embodiment 3
Above-mentioned light hydrocarbon recovery system is used in the hydroisomerizing system of white oil, low point of oily control temperature is 280 DEG C, entering lighter hydrocarbons recovery tower low point of oil mass is 24t/h, lighter hydrocarbons recovery column overhead temperatures is 170 DEG C, pressure is 0.25Mpa, through rectifying, gas phase portion arrives gas-liquid separator by tower top outlet through air cooler, water cooler twice condensation, and air cooler temperature is 90 DEG C; Water cooler water coolant is 20 DEG C; Gas-liquid separator temperature in is 60 DEG C; Dehydration position, circle is 50%, the lighter hydrocarbons that the gas phase of light hydrocarbon separator is recycled by light ends unit, and the outlet of light hydrocarbon separator oil phase is meticulous white oil.As calculated, the lighter hydrocarbons amount of recovery is 240NM
3/ h, the meticulous white oil amount of generation is 1.5t/h.
The above is only the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention; can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (10)
1. a light hydrocarbon recovery system, comprising:
Lighter hydrocarbons recovery tower;
Entrance exports with lighter hydrocarbons recovery column overhead the air cooler be connected, and described air cooler top is provided with temperature and controls executive device;
Entrance exports with air cooler the water cooler be connected;
Entrance exports with water cooler the light hydrocarbon separator be connected, and described light hydrocarbon separator is provided with temperature-control device;
The light ends unit that entrance is connected with light hydrocarbon separator pneumatic outlet.
2. light hydrocarbon recovery system according to claim 1, is characterized in that, the temperature-control device on described light hydrocarbon separator is be arranged at the threeway setting device between water cooler outlet and light hydrocarbon separator entrance.
3. light hydrocarbon recovery system according to claim 2, is characterized in that, described threeway setting device is connected with light hydrocarbon separator with water cooler, air cooler respectively.
4. light hydrocarbon recovery system according to claim 1, is characterized in that, described light hydrocarbon separator oil phase outlet is connected to lighter hydrocarbons recovery column overhead by transferpump.
5. adopt light hydrocarbon recovery system according to claim 1 to reclaim a method for lighter hydrocarbons, comprising:
Low point of oil enters lighter hydrocarbons recovery tower, and through rectifying, gas phase portion arrives light hydrocarbon separator by tower top outlet through air cooler, water cooler twice condensation, the lighter hydrocarbons that the gas phase lighter hydrocarbons of light hydrocarbon separator are recycled by light ends unit; The temperature out of described air cooler is 80 ~ 90 DEG C; The temperature in of described light hydrocarbon separator is 50 ~ 60 DEG C.
6. the method for recovery lighter hydrocarbons according to claim 5, is characterized in that, after described heating, low point of oily temperature is 270 ~ 300 DEG C.
7. the method for recovery lighter hydrocarbons according to claim 5, is characterized in that, the water temperature of described water cooler cooling water inlet is 0 ~ 32 DEG C.
8. the method for recovery lighter hydrocarbons according to claim 5, is characterized in that, the tower top temperature of described lighter hydrocarbons recovery tower is 160 ~ 180 DEG C.
9. the method for recovery lighter hydrocarbons according to claim 5, is characterized in that, the tower top pressure of described lighter hydrocarbons recovery tower is 0.2 ~ 0.25Mpa.
10. the method for recovery lighter hydrocarbons according to claim 5, is characterized in that, described light hydrocarbon separator dehydration position, circle 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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| CN201510974117.4A CN105567288B (en) | 2015-12-17 | 2015-12-17 | A kind of light hydrocarbon recovery system and method |
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| CN105567288A true CN105567288A (en) | 2016-05-11 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108165306A (en) * | 2016-12-06 | 2018-06-15 | 唐山宸午流体科技有限公司 | Soda acid processing complexes are exempted from the regeneration rectifying of extreme negative pressure waste oil catalytic pyrolysis |
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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 |
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| CN105567288B (en) | 2018-08-24 |
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