CN107603669A - The ethylene recovery system of catalytic cracked dry gas - Google Patents
The ethylene recovery system of catalytic cracked dry gas Download PDFInfo
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- CN107603669A CN107603669A CN201711016886.9A CN201711016886A CN107603669A CN 107603669 A CN107603669 A CN 107603669A CN 201711016886 A CN201711016886 A CN 201711016886A CN 107603669 A CN107603669 A CN 107603669A
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Abstract
The present invention relates to a kind of ethylene recovery system of catalytic cracked dry gas,Catalytic cracked dry gas is connected with water washing tank,Water washing tank outlet is connected with amine liquid absorber,The outlet of amine liquid absorber is connected with raw material surge tank,The outlet of raw material surge tank is connected with the cold side input port of First Heat Exchanger,The cold side outlet port of First Heat Exchanger is connected with the cold side input port of the second heat exchanger,The cold side outlet port of second heat exchanger is connected with raw materials furnace and heating entrance,Raw materials furnace and heating outlet is connected with the hot drying gas entrance at the top of catalytic reactor,The reactant exit of catalytic reactor bottom is connected with the hot side entrance of the second heat exchanger,The hot side outlet of second heat exchanger is connected with the lower entrances of fractionating column,The gaseous phase outlet of fractionating column and the hot side entrance of First Heat Exchanger connect,The heavy fuel oil export of fractionation column base is connected through the first cooler with heavy fuel oil pump,The outlet of heavy fuel oil pump is connected with heavy fuel oil tank.The system can directly generate fuel oil ingredient, liquefied petroleum gas components.
Description
Technical field
The present invention relates to a kind of ethylene recovery system of catalytic cracked dry gas, belong to oil refining technical field of auxiliary facilities.
Background technology
Catalytic cracking is one of main method of oil secondary operation.Make heavy fry dried food ingredients in the presence of high temperature and catalyst
Raw cracking reaction, it is changed into the process of cracked gas, gasoline and diesel oil etc..Key reaction has decomposition, isomerization, hydrogen migration, aromatization
Change, condensation, green coke etc..Compared with thermal cracking, its lightweight oily yield is high, and octane number is high, and diesel oil stability is preferable, and by-product
Liquefied gas rich in alkene.
The dry gas yied of existing catalytic cracking unit is 2 ~ 5%, contains the components such as hydrogen, ethene, methane, ethane in dry gas,
Wherein ethylene concentration is 15 ~ 25v%.In middle-size and small-size refinery, the dry gas of catalytic cracking unit enters combustion gas generally as fuel gas
Pipe network, for each unit furnace, boiler as fuel, residual fuel gas is then sent into flare system burn-up, causes ethene resource
Waste, while also pollute environment.
The content of the invention
It is an object of the present invention to overcome problems of the prior art, there is provided a kind of ethene of catalytic cracked dry gas
Recovery system, fuel oil ingredient, liquefied petroleum gas components can be directly generated.
For solve above technical problem, a kind of ethylene recovery system of catalytic cracked dry gas of the invention, including with catalysis
The catalytic cracked dry gas pipe G1 that the outlet of cracking dry gas is connected, the outlet of the catalytic cracked dry gas pipe G1 and entering for water washing tank V1
Mouth is connected, and water washing tank V1 outlet is connected with amine liquid absorber V2 entrance, amine liquid absorber V2 outlet and raw material surge tank
V3 entrance is connected, and raw material surge tank V3 outlet is connected with cold dry gas three-way pipeline G2, the cold dry gas three-way pipeline G2's
Upper port is connected with First Heat Exchanger H1 cold side input port, First Heat Exchanger H1 cold side outlet port and the second heat exchanger H2 cold side
Entrance connects, and the second heat exchanger H2 cold side outlet port is connected with raw materials furnace and heating F1 entrance, raw materials furnace and heating F1 outlet and
Hot drying gas entrance R1a at the top of catalytic reactor R1 is connected, the heat exchange of the reactant exit R1b of catalytic reactor R1 bottoms and second
Device H2 hot side entrance connection, the second heat exchanger H2 hot side outlet are connected with the blending ingredients entrance T1a of fractionating column T1 bottoms,
Fractionating column gaseous phase outlet T1d at the top of fractionating column T1 is connected with First Heat Exchanger H1 hot side entrance, the weight of fractionating column T1 bottoms
Matter fuel oil export T1b is connected through the first cooler L1 with heavy fuel oil pump P1 entrance, heavy fuel oil pump P1 outlet
It is connected with heavy fuel oil tank E1.
Relative to prior art, the present invention achieves following beneficial effect：In catalytic cracked dry gas containing hydrogen, ethene,
The components such as methane, ethane, wherein ethylene concentration are 15 ~ 25v%, and 0.5MPa, the catalytic cracked dry gas of normal temperature are from catalytic cracked dry gas
Pipe G1 is introduced into water washing tank V1 and washed, slightly the impurity such as de- monoethanolamine, subsequently into further being taken off in amine liquid absorber V2
Except remaining monoethanolamine, after the ammonia-nitrogen content in raw material dry gas is less than 100ppm, into raw material surge tank V3, raw material buffers
The cold dry gas of tank V3 outlets is tentatively preheated to 60 DEG C by First Heat Exchanger H1, then continues to be preheated to 90 by the second heat exchanger H2
~ 100 DEG C, reaction 240~280 DEG C of temperature of triggering is heated into raw materials furnace and heating F1, with the gradual intensification of reaction depth, heating
Heater outlet temperature is improved to 260~350 DEG C and stably.Hot drying gas enter catalytic reactor R1 from the hot drying gas entrance R1a at top
In, the temperature in catalytic reactor R1 is maintained at 260~380 DEG C, and pressure is maintained at 0.48MPa, and the ethene in hot drying gas is being urged
The reaction such as overlapping, cyclisation, dehydrogenation, hydrogen migration and isomerization occurs under agent effect in catalytic reactor R1, directly generates combustion
Expect oil ingredient and liquefied petroleum gas components.380 DEG C of catalytic reactor reaction products are discharged from catalytic reactor R1 bottom, are entered
Second heat exchanger H2 hot side, secondary preheating is carried out to the raw material dry gas by once preheating using the heat of reaction product, both
Raw materials furnace and heating F1 load is reduced, reduces its energy resource consumption, causes fuel oil ingredient and the liquefaction of catalytic reaction generation again
The temperature of petroleum gas components is down to 245 DEG C, is fractionated into fractionating column T1, and fractionating column T1 tower top pressure is controlled in 0.45MPa, point
Evaporate tower T1 tower top temperature control at 125 DEG C, fractionating column T1 column bottom temperature control at 225 DEG C, heavy fuel oil ingredient from point
The bottom of towe for evaporating tower T1 is extracted, and 40 DEG C are cooled to through the first cooler L1, is forced into 0.5MPa with heavy fuel oil pump P1, is delivered to
Heavy fuel oil tank E1 is stored, the first product after resulting in ethylene reaction and separating.120 DEG C of oil-gas component from
Fractionating column gaseous phase outlet T1d at the top of fractionating column T1 is steamed, and into First Heat Exchanger H1 hot side, utilizes the heat of oil-gas component
The raw material dry gas of normal temperature is once preheated, further reduces raw materials furnace and heating F1 load.The present invention utilizes 120 DEG C of oil
Gas component is once preheated to raw material dry gas, then carries out secondary preheating to raw material dry gas using 380 DEG C of reaction product, real
The raw material dry gas and the higher oil-gas component of temperature for having showed lowest temperature exchange heat, and the raw material dry gas after once preheating and temperature are higher
Reaction product exchanges heat, and overall is in countercurrent flow form, takes full advantage of the gradient difference of temperature, two-stage heat exchange is all maintained higher
Efficiency.
As the improvement of the present invention, the catalytic reactor R1 is sequentially provided with the first conversion zone, the second reaction from top to bottom
Section and the 3rd conversion zone, are provided with the first cold dry gas entrance R1c between the first conversion zone and the second conversion zone, the second conversion zone and the
The second cold dry gas entrance R1d is provided between three conversion zones, the first cold cold dry gas entrance R1d of dry gas entrance R1c and second divide
It is not connected in the lower port of the cold dry gas three-way pipeline G2.Catalytic reactor R1 sets three conversion zones from top to bottom, can be with
Make ethene in dry gas that catalytic reaction thoroughly occur；Because catalytic reaction is exothermic reaction, if can only be catalytic reactor R1's
Top carries out temperature control, and with flowing downward for unstripped gas, the temperature of the first to the 3rd conversion zone can produce very big difference,
It is unfavorable for the stable progress of reaction, between first and second conversion zone, the cold dry gas of raw material is passed through between second and third conversion zone, can be with
Each section in catalytic reactor R1 of reaction temperature is adjusted, prevents catalytic reactor R1 from temperature runaway occur.
As a further improvement on the present invention, First Heat Exchanger H1 hot side outlet and the second cooler L2 entrance phase
Even, the second cooler L2 outlet is connected with the oil water separator entrance V4a in the middle part of oil water separator V4, under oil water separator V4
The light Fuel oil export V4b in portion is connected with light Fuel oil pump P2 entrance, light Fuel oil pump P2 outlet respectively with gently
Matter fuel oil service tank E2 and fractionating column T1 fractionator overhead refluxing opening T1c is connected；Oil water separator V4 bottom discharge mouth V4c
It is connected by sewage pump P3 with sewage disposal system W1.From the oil-gas component that fractionating column gaseous phase outlet T1d is steamed in the first heat exchange
Device H1 hot side is carried out after once preheating to raw material dry gas, and temperature drops to 80 DEG C, is then cooled to 40 through the second cooler L2
DEG C, three phase separation is carried out using density contrast into oil water separator V4 middle parts, a small amount of sewage of oil water separator V4 bottoms is by dirt
Water pump P 3 is sent to sewage disposal system W1 processing, and light Fuel oil ingredient is assembled in oil water separator V4, separated, from profit point
Bottom discharge from device V4, then sent out by light Fuel oil pump P2, tower of a part of light Fuel oil ingredient as fractionating column T1
Top backflow enters fractionating column T1 from fractionator overhead refluxing opening T1c, and fractionating column T1 tower top temperature is accurately controlled in into 125 DEG C,
Another part delivers to light Fuel oil tank E2 storages, second of product after resulting in ethylene reaction and separating.
As a further improvement on the present invention, oil water separator V4 top lean gas exports V4c and lean gas surge tank V5's
Lower entrances are connected, and lean gas surge tank V5 top exit is connected with the first compressor C1 entrance, and the first compressor C1's goes out
Mouth is connected by the 3rd cooler L3 with the oil-trap entrance V6a on oil-trap V6 tops, the light-weight fuel oil of oil-trap V6 bottoms
Outlet V6b is connected with the oil water separator refluxing opening V4d of oil water separator V4 bottoms, and the oil water separator refluxing opening V4d exists
Short transverse is between the oil water separator entrance V4a and light Fuel oil export V4b；Oil-trap at the top of oil-trap V6
Exhaust outlet V6c is connected by lean gas return valve U1 with lean gas return duct G3, lean gas return duct G3 outlet and raw material surge tank V3
Entrance be connected.Oil water separator V4 top lean gas enters the first compressor C1 after lean gas surge tank V5 bufferings and compressed, the
Lean gas is pressurized to 0.6MPa by one compressor C1, is then cooled with circulating water to 40 DEG C through the 3rd cooler L3, is entered from oil-trap
Mouth V6a enters in oil-trap V6, a small amount of light-weight fuel oil carried in oil-trap V6 trapping lean gases, from the light of oil-trap V6 bottoms
Matter fuel oil export V6b is discharged, and is back to from oil water separator refluxing opening V4d in oil water separator V4, due to oil-trap V6
Moisture content is extremely low in the light-weight fuel oil of trapping, and oil water separator V4 oil water separator refluxing opening V4d is located at oil water separator
Between entrance V4a and light Fuel oil export V4b so that the light-weight fuel oil of oil-trap V6 trappings is directly entered oil water separator
V4 oil phase space, directly sent out or flowed back by light Fuel oil pump P2.The lean gas of part discharge at the top of oil-trap V6
After being mixed by lean gas return valve U1 and lean gas return duct G3 with pretreated raw material dry gas, enter raw material surge tank jointly
V3, by the ethylene concentration control for entering catalytic reactor R1 10~20%, the fluctuation of concentration of unstripped gas is compensated, ensures recovery system
The stable operation of system.
As a further improvement on the present invention, the oil-trap exhaust outlet V6c at the top of oil-trap V6 also passes through lean gas drain valve
U2 is connected with coalescing filter Y1 entrance, coalescing filter Y1 outlet preheated device H4 and one-level seperation film group X1's
Entrance is connected, and the one-level offgas outlet X1a at the top of one-level seperation film group X1 is connected with the second-order separation film group X2 entrance, two fractions
Two level offgas outlet X2a from film group X2 is connected by gas pipeline G4 with gas ductwork E3.Discharged from oil-trap exhaust outlet V6c
Lean gas liquefied petroleum gas separating system is also entered by lean gas drain valve U2, first pass through coalescing filter Y1 except deentrainment
Drop and impurity, then preheated device H4 are preheated to 40~50 DEG C, one-level permeability and separation are carried out into one-level seperation film group X1, from one
The one-level tail gas of level offgas outlet X1a discharges enters the second-order separation film group X2 and carries out two level permeability and separation, from two level offgas outlet
X2a discharge two level tail gas for poor light hydrocarbon component as the third product separated, be sent to gas ductwork E3 conducts
Fuel uses；Propane, propylene, butane, butylene etc. can vaporize at 40~50 DEG C, avoid liquid phase substance from being bonded in seperation film
Surface, to improve osmotic effect.
As a further improvement on the present invention, one-level seperation film group X1 one-level oozes vent outlet X1b and the second-order separation film
Group X2 two level is oozed vent outlet X2b and is connected respectively with permeating gas surge tank V7 entrance, infiltration gas surge tank V7 outlet with
Second compressor C2 entrance is connected, and the second compressor C2 outlet is connected with compressed gas surge tank V8 entrance, and compressed gas delays
Rush tank V8 outlet with the absorption tower infiltration gas entrance T2a of diesel oil absorption tower T2 bottoms to be connected, the suction of diesel oil absorption tower T2 bottoms
Receive tower outlet T2b with the desorber entrance T3a in the middle part of desorber T3 to be connected, the desorber gaseous phase outlet T3c at the top of desorber T3
It is connected by the 4th cooler L4 with liquefied petroleum gas surge tank V9 entrance, liquefied petroleum gas surge tank V9 outlet and liquefaction
Petroleum gas pump P4 entrance is connected, and liquefied petroleum gas pump P4 outlet is connected with liquefied petroleum gas storage tank E4.One-level seperation film group
The infiltration atmospheric pressure rich in lighter hydrocarbons that X1 and the second-order separation film group X2 are penetrated is 0.05MPa, oozes vent outlet X1b from one-level
Vent outlet X2b is oozed with two level and respectively enters infiltration gas surge tank V7, then liquid is turned into by the second compressor C2 pressure-raisings to 1.0MPa
State, after compressed gas surge tank V8 is temporary, from absorption tower, infiltration gas entrance T2a enters diesel oil absorption tower T2 bottom, with absorption
40 DEG C of diesel oil counter current contactings that column overhead enters, diesel oil absorb the liquefied petroleum gas components in infiltration gas during flowing downward,
The desorber entrance T3a that 42 DEG C diesel oil of the bottom of towe rich in liquefied petroleum gas components are sent into the middle part of desorber T3 carries out spray desorption,
Liquefied petroleum gas components are discharged from the desorber gaseous phase outlet T3c at the top of desorber T3, and 40 DEG C are cooled to through the 4th cooler L4,
Kept in into liquefied petroleum gas surge tank V9, extracted out by liquefied petroleum gas pump P4 and boost to 1.2MPa, a part is as separation
The 4th kind of product gone out is sent to liquefied petroleum gas storage tank E4 storages.
As a further improvement on the present invention, liquefied petroleum gas pump P4 outlet also by liquefied petroleum gas return duct G5 with
The desorber refluxing opening T3d of desorber T3 tower tops is connected；Desorber T3 bottoms are provided with reboiler, the desorber bavin of desorber T3 bottoms
Oil export T3b is connected with diesel pump P5 entrance, and diesel pump P5 outlet is connected with diesel return pipe G6, diesel return pipe G6's
Outlet is connected with the 3rd heat exchanger H3 hot side entrance, the 3rd heat exchanger H3 hot side outlet and the suction of diesel oil absorption tower T2 tower tops
Tower refluxing opening T2d is received to be connected；Absorption tower the outlet T2b and the 3rd heat exchanger H3 of diesel oil absorption tower T2 bottoms cold side input port phase
Even, the 3rd heat exchanger H3 cold side outlet port is connected with the desorber entrance T3a in the middle part of desorber T3.Liquefied petroleum gas pump P4 is by liquid
Liquefied oil gas component boosts to 1.2MPa and part is back to desorber T3 tower top from desorber refluxing opening T3d and sprayed,
Recycle, and desorber T3 tower top temperature is controlled at 50 DEG C.The reboiler at desorber T3 bottoms is made using 0.3MPa steam
For thermal source, the temperature for controlling desorber bottom is 102 DEG C, and diesel pump P5 boosts to the hot side that 1.2MPa is sent into the 3rd heat exchanger H3,
Indirect heat exchange is carried out with the rich diesel oil of cold side, on the one hand reclaims the heat in hot side diesel oil, is improved into desorber entrance T3a's
The temperature of rich diesel oil, reduces desorber T3 energy consumption, on the other hand causes the diesel oil of desorber diesel oil outlet T3b discharges through the 3rd
Enter the absorption tower refluxing opening T2d of diesel oil absorption tower T2 tower tops after heat exchanger H3 coolings, recycle, and control diesel oil absorption tower
T2 tower top temperature is 40 DEG C.
As a further improvement on the present invention, the absorption tower gaseous phase outlet T2c at the top of the T2 of diesel oil absorption tower passes through Gas Pipe
Road G4 is connected with gas ductwork E3.In the T2 of diesel oil absorption tower not by the residual gas of diesel oil absorption at the top of the T2 of diesel oil absorption tower
Absorption tower gaseous phase outlet T2c is discharged, and also serves as the third product separated, be sent to gas ductwork E3 makes as fuel
With, thus achieve resource all of realizing the zero-emission of pollutant.
As a further improvement on the present invention, ethylene concentration detection is installed on the outlet conduit of the raw material surge tank V3
Instrument S1, the lean gas return valve U1 aperture are controlled by the ethylene concentration value that the ethylene concentration survey meter S1 is detected.According to
The aperture for the ethylene concentration value control lean gas return valve U1 that ethylene concentration survey meter S1 is detected, by raw material surge tank V3 outlets
Ethylene concentration control ensures the stable operation of whole dry-gas recovery system 10~20%.
As a further improvement on the present invention, cooling water system is also connected with cold including cooling tower T4, the cooling tower T4
But tower upper hose G7 and cooling tower downcomer G8；Cooling tower downcomer G8 outlet and the 3rd cooler L3 cooling water inlet phase
Even, the 3rd cooler L3 coolant outlet is connected with the hot side import of the preheater H4, and the hot side of the preheater H4 goes out
Mouth is connected with cooling water circulating pump P6 entrance, the outlet of the cooling water circulating pump P6 and the cooling tower upper hose G7 phases
Even.It is poor to being compressed through the first compressor C1 that the 3rd cooler L3 is introduced into from the low-temperature cooling water of cooling tower downcomer G8 outflows
Gas is cooled down, and lean gas temperature is down into 40 DEG C by 100 DEG C, the coolant water temperature discharged from the 3rd cooler L3 coolant outlet
Up to 75 DEG C of degree, into preheater H4 hot side, the preheated device H4 of heat convection contained using the high-temperature cooling water lean gas
Preheated, lean gas is preheated into 40~50 DEG C enters one-level seperation film group X1 progress one-level permeability and separations, both realizes high temperature
The UTILIZATION OF VESIDUAL HEAT IN of cooling water, the load of cooling tower is reduced again, while the lean gas to entering seperation film is preheated, and is reduced
The energy consumption of whole system.
Brief description of the drawings
The present invention is further detailed explanation with reference to the accompanying drawings and detailed description, accompanying drawing only provide with reference to
Illustrate to use, be not used to the limitation present invention.
Fig. 1 is the flow chart of the ethylene recovery system embodiment one of catalytic cracked dry gas of the present invention.
Fig. 2 is the afterheat utilizing system figure of the 3rd heat exchanger cooling water in Fig. 1.
Fig. 3 is the flow chart of the ethylene recovery system embodiment two of catalytic cracked dry gas of the present invention.
Fig. 4 is the flow chart of the ethylene recovery system embodiment three of catalytic cracked dry gas of the present invention.
In figure：V1. water washing tank；V2. amine liquid absorber；V3. raw material surge tank；V4. oil water separator；V5. lean gas buffers
Tank；V6. oil-trap；V7. gas surge tank is permeated；V8. compressed gas surge tank；V9. liquefied petroleum gas surge tank；R1. catalytic reaction
Device；R1a. hot drying gas entrance；R1b. reactant exit；R1c. the first cold dry gas entrance；R1d. the second cold dry gas entrance；F1. it is former
Expect heating furnace；H1. First Heat Exchanger；H2. the second heat exchanger；H3. the 3rd heat exchanger；H4. preheater；T1. fractionating column；T1a. mix
Charge-coupled subentry；T1b. heavy fuel oil export；T1c. fractionator overhead refluxing opening；T1d. fractionating column gaseous phase outlet；T2. diesel oil
Absorption tower；T2a. absorption tower infiltration gas entrance；T2b. absorption tower exports；T2c. absorption tower gaseous phase outlet；T2d. absorption tower is flowed back
Mouthful；T3. desorber；T3a. desorber entrance；T3b. desorber diesel oil exports；T3c. desorber gaseous phase outlet；T3d. desorber
Refluxing opening；T4. cooling tower；Y1. coalescing filter；L1. the first cooler；L2. the second cooler；L3. the 3rd cooler；
L4. the 4th cooler；C1. the first compressor；C2. the second compressor；P1. heavy fuel oil pump；P2. light Fuel oil pump；P3.
Sewage pump；P4. liquefied petroleum gas pump；P5. diesel pump；P6. cooling water circulating pump；X1. one-level seperation film group；X2. the second-order separation
Film group；G1. raw material feed channel；G2. cold dry gas three-way pipeline；G3. lean gas return duct；G4. gas pipeline；G5. liquefied petroleum gas
Return duct；G6. diesel return pipe；G7. cooling tower upper hose；G8. cooling tower downcomer；E1. heavy fuel oil tank；E2. it is light
Matter fuel oil service tank；E3. gas ductwork；E4. liquefied petroleum gas storage tank；W1. sewage disposal system；U1. lean gas return valve；U2.
Lean gas drain valve；S1. ethylene concentration survey meter.
Embodiment
As shown in figure 1, the ethylene recovery system of catalytic cracked dry gas of the present invention, including be connected with catalytic cracked dry gas outlet
The catalytic cracked dry gas pipe G1 connect, catalytic cracked dry gas pipe G1 outlet are connected with water washing tank V1 entrance, and water washing tank V1's goes out
Mouth is connected with amine liquid absorber V2 entrance, and amine liquid absorber V2 outlet is connected with raw material surge tank V3 entrance, and raw material delays
The outlet for rushing tank V3 is connected with cold dry gas three-way pipeline G2, and cold dry gas three-way pipeline G2 upper port is cold with First Heat Exchanger H1's
Side entrance is connected, and First Heat Exchanger H1 cold side outlet port is connected with the second heat exchanger H2 cold side input port, the second heat exchanger H2's
Cold side outlet port is connected with raw materials furnace and heating F1 entrance, raw materials furnace and heating F1 outlet and the hot drying gas at the top of catalytic reactor R1
Entrance R1a is connected, and the reactant exit R1b of catalytic reactor R1 bottoms is connected with the second heat exchanger H2 hot side entrance, and second
Heat exchanger H2 hot side outlet is connected with the blending ingredients entrance T1a of fractionating column T1 bottoms, the fractionating column gas at the top of fractionating column T1
Mutually outlet T1d is connected with First Heat Exchanger H1 hot side entrance, and the heavy fuel oil export T1b of fractionating column T1 bottoms is cold through first
But device L1 is connected with heavy fuel oil pump P1 entrance, and heavy fuel oil pump P1 outlet is connected with heavy fuel oil tank E1.
Containing components such as hydrogen, ethene, methane, ethane in catalytic cracked dry gas, wherein ethylene concentration is 15 ~ 25v%,
0.5MPa, the catalytic cracked dry gas of normal temperature are introduced into water washing tank V1 from catalytic cracked dry gas pipe G1 and washed, and slightly take off ethanol
The impurity such as amine, subsequently into remaining monoethanolamine is further removed in amine liquid absorber V2, make the ammonia-nitrogen content in raw material dry gas
After 100ppm, into raw material surge tank V3, the cold dry gas of raw material surge tank V3 outlets is preliminary by First Heat Exchanger H1
60 DEG C are preheated to, then continues to be preheated to 90 ~ 100 DEG C by the second heat exchanger H2, being heated to reaction into raw materials furnace and heating F1 touches
240~280 DEG C of temperature is sent out, with the gradual intensification of reaction depth, furnace outlet temperature is improved to 260~350 DEG C and stably.Heat
Dry gas enters in catalytic reactor R1 from the hot drying gas entrance R1a at top, and the temperature in catalytic reactor R1 is maintained at 260~
380 DEG C, pressure is maintained at 0.48MPa, the ethene in hot drying gas occur under catalyst action in catalytic reactor R1 overlapping,
Cyclisation, dehydrogenation, hydrogen migration and isomerization etc. are reacted, and directly generate fuel oil ingredient and liquefied petroleum gas components.
380 DEG C of catalytic reactor reaction products are discharged from catalytic reactor R1 bottom, into the second heat exchanger H2 heat
Side, using the heat of reaction product to carrying out secondary preheating by the raw material dry gas once preheated, both reduce raw materials furnace and heating
F1 load, its energy resource consumption is reduced, cause the fuel oil ingredient of catalytic reaction generation and the temperature of liquefied petroleum gas components again
245 DEG C are down to, is fractionated into fractionating column T1, fractionating column T1 tower top pressure is controlled in 0.45MPa, fractionating column T1 tower top temperature
Control is at 125 DEG C, and fractionating column T1 column bottom temperature is controlled at 225 DEG C, and heavy fuel oil ingredient is taken out from fractionating column T1 bottom of towe
Go out, 40 DEG C are cooled to through the first cooler L1, be forced into 0.5MPa with heavy fuel oil pump P1, deliver to heavy fuel oil tank E1
Storage, the first product after resulting in ethylene reaction and separating.
120 DEG C of oil-gas component steams from the fractionating column gaseous phase outlet T1d at the top of fractionating column T1, into First Heat Exchanger H1
Hot side, the raw material dry gas of normal temperature is once preheated using the heat of oil-gas component, further reduces raw materials furnace and heating F1
Load.The present invention is once preheated using 120 DEG C of oil-gas component to raw material dry gas, is then produced using 380 DEG C of reaction
Thing carries out secondary preheating to raw material dry gas, and the raw material dry gas and the higher oil-gas component of temperature for realizing lowest temperature exchange heat, once
Raw material dry gas after preheating exchanges heat with the higher reaction product of temperature, and overall is in countercurrent flow form, takes full advantage of temperature
Gradient difference, two-stage heat exchange is set all to maintain higher efficiency.
Catalytic reactor R1 is sequentially provided with the first conversion zone, the second conversion zone and the 3rd conversion zone from top to bottom, and first is anti-
Answer and the first cold dry gas entrance R1c is provided between section and the second conversion zone, second is provided between the second conversion zone and the 3rd conversion zone
Cold dry gas entrance R1d, the first cold cold dry gas entrance R1d of dry gas entrance R1c and second are respectively under cold dry gas three-way pipeline G2
Port is connected.Catalytic reactor R1 sets three conversion zones from top to bottom, can make ethene in dry gas that catalytic reaction thoroughly occur；
Because catalytic reaction is exothermic reaction, if temperature control can only be carried out at catalytic reactor R1 top, with unstripped gas
Flowing downward, the temperature of the first to the 3rd conversion zone can produce very big difference, be unfavorable for the stable progress of reaction, first,
Between two conversion zones, the cold dry gas of raw material is passed through between second and third conversion zone, each section in catalytic reactor R1 of reaction can be adjusted
Temperature, prevent catalytic reactor R1 from temperature runaway occur.
First Heat Exchanger H1 hot side outlet is connected with the second cooler L2 entrance, the second cooler L2 outlet and oil
Oil water separator entrance V4a in the middle part of separator V4 is connected, the light Fuel oil export V4b of oil water separator V4 bottoms with it is light
Matter fuel pump P2 entrance is connected, and light Fuel oil pump P2 outlet is respectively with light Fuel oil tank E2's and fractionating column T1
Fractionator overhead refluxing opening T1c is connected；Oil water separator V4 bottom discharge mouth V4c passes through sewage pump P3 and sewage disposal system
W1 is connected.
Hot side from the oil-gas component that fractionating column gaseous phase outlet T1d is steamed in First Heat Exchanger H1 carries out one to raw material dry gas
After secondary preheating, temperature drops to 80 DEG C, is then cooled to 40 DEG C through the second cooler L2, is utilized into oil water separator V4 middle parts
Density contrast carries out three phase separation, and a small amount of sewage of oil water separator V4 bottoms is sent to sewage disposal system W1 by sewage pump P3
Reason, light Fuel oil ingredient are assembled in oil water separator V4, separated, and are discharged from oil water separator V4 bottom, then by lightweight
Fuel pump P2 is sent out, a part of light Fuel oil ingredient as fractionating column T1 overhead reflux from fractionator overhead refluxing opening
T1c enters fractionating column T1, fractionating column T1 tower top temperature is accurately controlled in into 125 DEG C, another part delivers to light-weight fuel oil storage
Tank E2 is stored, second of product after resulting in ethylene reaction and separating.
Oil water separator V4 top lean gas outlet V4c is connected with lean gas surge tank V5 lower entrances, lean gas surge tank
V5 top exit is connected with the first compressor C1 entrance, and oil by the 3rd cooler L3 and is caught in the first compressor C1 outlet
The oil-trap entrance V6a on device V6 tops is connected, light Fuel oil export V6b and oil water separator the V4 bottom of oil-trap V6 bottoms
Oil water separator refluxing opening V4d be connected, oil water separator refluxing opening V4d is located at oil water separator entrance V4a in short transverse
Between light Fuel oil export V4b；Oil-trap exhaust outlet V6c at the top of oil-trap V6 is returned by lean gas return valve U1 and lean gas
Flow tube G3 is connected, and lean gas return duct G3 outlet is connected with raw material surge tank V3 entrance.
Oil water separator V4 top lean gas enters the first compressor C1 after lean gas surge tank V5 bufferings and compressed, the first pressure
Lean gas is pressurized to 0.6MPa by contracting machine C1, is then cooled with circulating water through the 3rd cooler L3 to 40 DEG C, from oil-trap entrance V6a
Into in oil-trap V6, oil-trap V6 traps a small amount of light-weight fuel oil carried in lean gas, is fired from the lightweight of oil-trap V6 bottoms
Expect oil export V6b discharges, and be back to from oil water separator refluxing opening V4d in oil water separator V4, because oil-trap V6 is trapped
Light-weight fuel oil in moisture content it is extremely low, oil water separator V4 oil water separator refluxing opening V4d is located at oil water separator entrance
Between V4a and light Fuel oil export V4b so that the light-weight fuel oil of oil-trap V6 trappings is directly entered oil water separator V4's
Oil phase space, directly sent out or flowed back by light Fuel oil pump P2.Part lean gas of discharge at the top of oil-trap V6 passes through
After lean gas return valve U1 and lean gas return duct G3 mixes with pretreated raw material dry gas, enter raw material surge tank V3 jointly, will
Into catalytic reactor R1 ethylene concentration control 10~20%, compensate the fluctuation of concentration of unstripped gas, ensure the steady of recovery system
Fixed operation.
Oil-trap exhaust outlet V6c at the top of oil-trap V6 also passes through lean gas drain valve U2 and coalescing filter Y1 entrance
It is connected, the coalescing filter Y1 preheated device H4 in outlet is connected with one-level seperation film group X1 entrance, one-level seperation film group X1
The one-level offgas outlet X1a at top is connected with the second-order separation film group X2 entrance, the second-order separation film group X2 two level offgas outlet
X2a is connected by gas pipeline G4 with gas ductwork E3.Also pass through lean gas drain valve from the lean gas of oil-trap exhaust outlet V6c discharges
U2 enters liquefied petroleum gas separating system, first passes through drop and impurity that coalescing filter Y1 removes deentrainment, then preheated device
H4 is preheated to 40~50 DEG C, and one-level permeability and separation is carried out into one-level seperation film group X1, from the one of one-level offgas outlet X1a discharges
Level tail gas enters the second-order separation film group X2 and carries out two level permeability and separation, and the two level tail gas from two level offgas outlet X2a discharges is
Poor light hydrocarbon component is sent to gas ductwork E3 and used as fuel as the third product separated.
The two level that one-level seperation film group X1 one-level oozes vent outlet X1b and the second-order separation film group X2 oozes vent outlet X2b
It is connected respectively with permeating gas surge tank V7 entrance, infiltration gas surge tank V7 outlet is connected with the second compressor C2 entrance,
Second compressor C2 outlet is connected with compressed gas surge tank V8 entrance, compressed gas surge tank V8 outlet and diesel oil absorption tower
The absorption tower infiltration gas entrance T2a of T2 bottoms is connected, in the middle part of the absorption tower outlet T2b and desorber T3 of diesel oil absorption tower T2 bottoms
Desorber entrance T3a be connected, the desorber gaseous phase outlet T3c at the top of desorber T3 passes through the 4th cooler L4 and liquefied petroleum
Gas surge tank V9 entrance is connected, and liquefied petroleum gas surge tank V9 outlet is connected with liquefied petroleum gas pump P4 entrance, liquefaction
Petroleum gas pump P4 outlet is connected with liquefied petroleum gas storage tank E4.
The infiltration atmospheric pressure rich in lighter hydrocarbons that one-level seperation film group X1 and the second-order separation film group X2 are penetrated is 0.05MPa,
Ooze vent outlet X1b from one-level and ooze vent outlet X2b with two level and respectively enter and permeate gas surge tank V7, then by the second compressor C2
Pressure-raising turns into liquid to 1.0MPa, after compressed gas surge tank V8 is temporary, permeates gas entrance T2a from absorption tower and is absorbed into diesel oil
Tower T2 bottom, the 40 DEG C of diesel oil counter current contactings entered with absorbing tower jacking, diesel oil are absorbed during flowing downward in infiltration gas
Liquefied petroleum gas components, the desorber entrance that 42 DEG C diesel oil of the bottom of towe rich in liquefied petroleum gas components are sent into the middle part of desorber T3
T3a carries out spray desorption, and liquefied petroleum gas components are cold through the 4th from the desorber gaseous phase outlet T3c discharges at the top of desorber T3
But device L4 is cooled to 40 DEG C, is kept in into liquefied petroleum gas surge tank V9, is extracted out and is boosted to by liquefied petroleum gas pump P4
1.2MPa, a part are sent to liquefied petroleum gas storage tank E4 storages as the 4th kind of product isolated.
Liquefied petroleum gas pump P4 outlet is also returned by the desorber of liquefied petroleum gas return duct G5 and desorber T3 tower tops
Head piece T3d is connected；Desorber T3 bottoms are provided with reboiler, the desorber diesel oil outlet T3b and diesel pump P5's of desorber T3 bottoms
Entrance is connected, and diesel pump P5 outlet is connected with diesel return pipe G6, and diesel return pipe G6 outlet is with the 3rd heat exchanger H3's
Hot side entrance is connected, and the 3rd heat exchanger H3 hot side outlet is connected with the absorption tower refluxing opening T2d of diesel oil absorption tower T2 tower tops；Bavin
The absorption tower outlet T2b of oil-absorption tower T2 bottoms is connected with the 3rd heat exchanger H3 cold side input port, the 3rd heat exchanger H3 cold side
Outlet is connected with the desorber entrance T3a in the middle part of desorber T3.
Liquefied petroleum gas components are boosted to liquefied petroleum gas pump P4 into 1.2MPa and part is flowed back from desorber refluxing opening T3d
Tower top to desorber T3 is sprayed, and is recycled, and desorber T3 tower top temperature is controlled at 50 DEG C.Desorber T3 bottoms
Reboiler using 0.3MPa steam be used as thermal source, control desorber bottom temperature be 102 DEG C, diesel pump P5 boosts to 1.2MPa
The 3rd heat exchanger H3 hot side is sent into, indirect heat exchange is carried out with the rich diesel oil of cold side, on the one hand reclaims the heat in hot side diesel oil,
The temperature into desorber entrance T3a rich diesel oil is improved, desorber T3 energy consumption is reduced, on the other hand causes desorber diesel oil
The diesel oil for exporting T3b discharges enters the absorption tower refluxing opening T2d of diesel oil absorption tower T2 tower tops after the 3rd heat exchanger H3 coolings, follows
Ring use, and control diesel oil absorption tower T2 tower top temperature be 40 DEG C.
Absorption tower gaseous phase outlet T2c at the top of the T2 of diesel oil absorption tower is connected by gas pipeline G4 with gas ductwork E3.Bavin
Do not discharged in oil-absorption tower T2 by the residual gas that diesel oil absorbs from the absorption tower gaseous phase outlet T2c at the top of the T2 of diesel oil absorption tower,
The third product separated is also served as, gas ductwork E3 is sent to and is used as fuel, thus achieve the whole of resource
Utilize, realize the zero-emission of pollutant.
Ethylene concentration survey meter S1 is installed, lean gas return valve U1 aperture is controlled on raw material surge tank V3 outlet conduit
In the ethylene concentration value that ethylene concentration survey meter S1 is detected.The ethylene concentration value control detected according to ethylene concentration survey meter S1
Lean gas return valve U1 processed aperture, by the ethylene concentration control of raw material surge tank V3 outlets 10~20%, ensure that whole dry gas returns
The stable operation of receipts system.
As shown in Fig. 2 each cooler is provided with cooling tower T4, cooling tower using cooling water as medium, cooling water system
T4 is connected with cooling tower upper hose G7 and cooling tower downcomer G8；Cooling tower downcomer G8 outlet is cold with the 3rd cooler L3's
But water inlet is connected, and the 3rd cooler L3 coolant outlet is connected with preheater H4 hot side import, preheater H4 hot side
Outlet is connected with cooling water circulating pump P6 entrance, and cooling water circulating pump P6 outlet is connected with cooling tower upper hose G7.
The 3rd cooler L3 is introduced into being pressed through the first compressor C1 from the low-temperature cooling water of cooling tower downcomer G8 outflows
The lean gas of contracting is cooled down, and lean gas temperature is down into 40 DEG C by 100 DEG C, is discharged from the 3rd cooler L3 coolant outlet cold
But coolant-temperature gage is up to 75 DEG C, into preheater H4 hot side, the preheated device H4 of heat convection contained using the high-temperature cooling water
Lean gas preheated, lean gas be preheated to 40~50 DEG C enter one-level seperation film group X1 and carry out one-level permeability and separations, both realized
The UTILIZATION OF VESIDUAL HEAT IN of high-temperature cooling water, the load of cooling tower is again reduced, while the lean gas to entering seperation film is preheated,
Reduce the energy consumption of whole system.
Fig. 3 show another embodiment of the present invention, and the cold dry gas of raw material surge tank V3 outlets is without the first heat exchange
Device H1, only exchanged heat by the second heat exchanger H2.Remaining is identical with embodiment one.
Fig. 4 show another embodiment of the present invention, the 3rd heat exchanger H3 cold side not Fu Chai with absorption tower discharge
Oil carries out indirect heat exchange, but is passed through cooling water and the diesel oil of desorber diesel oil outlet T3b discharges is cooled down, remaining and implementation
Example one is identical.
It the foregoing is only the preferable possible embodiments of the present invention, non-therefore the limitation present invention patent protection model
Enclose.In addition to the implementation, the present invention can also have other embodiment.All skills formed using equivalent substitution or equivalent transformation
Art scheme, all falls within the protection domain of application claims.Technical characteristic of the invention without description can be by or using now
There is technology realization, will not be repeated here.
Claims (10)
1. a kind of ethylene recovery system of catalytic cracked dry gas, including done with the catalytic cracking that catalytic cracked dry gas outlet is connected
Tracheae（G1）, it is characterised in that the catalytic cracked dry gas pipe（G1）Outlet and water washing tank（V1）Entrance be connected, water washing tank
（V1）Outlet and amine liquid absorber（V2）Entrance be connected, amine liquid absorber（V2）Outlet and raw material surge tank（V3）Enter
Mouth is connected, raw material surge tank（V3）Outlet and cold dry gas three-way pipeline（G2）It is connected, the cold dry gas three-way pipeline（G2）'s
Upper port and First Heat Exchanger（H1）Cold side input port connection, First Heat Exchanger（H1）Cold side outlet port and the second heat exchanger（H2）
Cold side input port connection, the second heat exchanger（H2）Cold side outlet port and raw materials furnace and heating（F1）Entrance be connected, raw materials furnace and heating
（F1）Outlet and catalytic reactor（R1）The hot drying gas entrance at top（R1a）It is connected, catalytic reactor（R1）The reaction of bottom
Thing exports（R1b）With the second heat exchanger（H2）Hot side entrance connection, the second heat exchanger（H2）Hot side outlet and fractionating column
（T1）The blending ingredients entrance of bottom（T1a）It is connected, fractionating column（T1）The fractionating column gaseous phase outlet at top（T1d）With the first heat exchange
Device（H1）Hot side entrance connection, fractionating column（T1）The heavy fuel oil export of bottom（T1b）Through the first cooler（L1）With again
Matter fuel pump（P1）Entrance be connected, heavy fuel oil pump（P1）Outlet and heavy fuel oil tank（E1）It is connected.
2. the ethylene recovery system of catalytic cracked dry gas according to claim 1, it is characterised in that：The catalytic reactor
（R1）The first conversion zone, the second conversion zone and the 3rd conversion zone, the first conversion zone and the second conversion zone are sequentially provided with from top to bottom
Between be provided with the first cold dry gas entrance（R1c）, the second cold dry gas entrance is provided between the second conversion zone and the 3rd conversion zone
（R1d）, the first cold dry gas entrance（R1c）With the second cold dry gas entrance（R1d）Respectively at the cold dry gas three-way pipeline
（G2）Lower port be connected.
3. the ethylene recovery system of catalytic cracked dry gas according to claim 1, it is characterised in that：First Heat Exchanger（H1）
Hot side outlet and the second cooler（L2）Entrance be connected, the second cooler（L2）Outlet and oil water separator（V4）Middle part
Oil water separator entrance（V4a）It is connected, oil water separator（V4）The light Fuel oil export of bottom（V4b）With light-weight fuel oil
Pump（P2）Entrance be connected, light Fuel oil pump（P2）Outlet respectively with light Fuel oil tank（E2）And fractionating column（T1）'s
Fractionator overhead refluxing opening（T1c）It is connected；Oil water separator（V4）Bottom discharge mouth（V4c）Pass through sewage pump（P3）With sewage
Processing system（W1）It is connected.
4. the ethylene recovery system of catalytic cracked dry gas according to claim 3, it is characterised in that：Oil water separator（V4）
The outlet of top lean gas（V4c）With lean gas surge tank（V5）Lower entrances be connected, lean gas surge tank（V5）Top exit with
First compressor（C1）Entrance be connected, the first compressor（C1）Outlet pass through the 3rd cooler（L3）With oil-trap（V6）On
The oil-trap entrance in portion（V6a）It is connected, oil-trap（V6）The light Fuel oil export of bottom（V6b）With oil water separator（V4）Under
The oil water separator refluxing opening in portion（V4d）It is connected, the oil water separator refluxing opening（V4d）It is located at the profit in short transverse
Separator inlet（V4a）With light Fuel oil export（V4b）Between；Oil-trap（V6）The oil-trap exhaust outlet at top（V6c）It is logical
Cross lean gas return valve（U1）With lean gas return duct（G3）It is connected, lean gas return duct（G3）Outlet and raw material surge tank（V3）Enter
Mouth is connected.
5. the ethylene recovery system of catalytic cracked dry gas according to claim 4, it is characterised in that：Oil-trap（V6）Top
Oil-trap exhaust outlet（V6c）Also pass through lean gas drain valve（U2）With coalescing filter（Y1）Entrance be connected, coagulation type mistake
Filter（Y1）The preheated device in outlet（H4）With one-level seperation film group（X1）Entrance be connected, one-level seperation film group（X1）Top
One-level offgas outlet（X1a）With the second-order separation film group（X2）Entrance be connected, the second-order separation film group（X2）Two level offgas outlet
（X2a）Pass through gas pipeline（G4）With gas ductwork（E3）It is connected.
6. the ethylene recovery system of catalytic cracked dry gas according to claim 5, it is characterised in that：One-level seperation film group
（X1）One-level ooze vent outlet（X1b）With the second-order separation film group（X2）Two level ooze vent outlet（X2b）Respectively with permeating gas
Surge tank（V7）Entrance be connected, permeate gas surge tank（V7）Outlet and the second compressor（C2）Entrance be connected, second pressure
Contracting machine（C2）Outlet and compressed gas surge tank（V8）Entrance be connected, compressed gas surge tank（V8）Outlet and diesel oil absorption tower
（T2）The absorption tower infiltration gas entrance of bottom（T2a）It is connected, diesel oil absorption tower（T2）The absorption tower outlet of bottom（T2b）With desorption
Tower（T3）The desorber entrance at middle part（T3a）It is connected, desorber（T3）The desorber gaseous phase outlet at top（T3c）It is cold by the 4th
But device（L4）With liquefied petroleum gas surge tank（V9）Entrance be connected, liquefied petroleum gas surge tank（V9）Outlet and liquefied petroleum
Air pump（P4）Entrance be connected, liquefied petroleum gas pump（P4）Outlet and liquefied petroleum gas storage tank（E4）It is connected.
7. the ethylene recovery system of catalytic cracked dry gas according to claim 6, it is characterised in that：Liquefied petroleum gas pump
（P4）Outlet also pass through liquefied petroleum gas return duct（G5）With desorber（T3）The desorber refluxing opening of tower top（T3d）It is connected；
Desorber（T3）Bottom is provided with reboiler, desorber（T3）The desorber diesel oil outlet of bottom（T3b）With diesel pump（P5）Entrance
It is connected, diesel pump（P5）Outlet and diesel return pipe（G6）It is connected, diesel return pipe（G6）Outlet and the 3rd heat exchanger
（H3）Hot side entrance be connected, the 3rd heat exchanger（H3）Hot side outlet and diesel oil absorption tower（T2）The absorption tower refluxing opening of tower top
（T2d）It is connected；Diesel oil absorption tower（T2）The absorption tower outlet of bottom（T2b）With the 3rd heat exchanger（H3）Cold side input port be connected,
3rd heat exchanger（H3）Cold side outlet port and desorber（T3）The desorber entrance at middle part（T3a）It is connected.
8. the ethylene recovery system of catalytic cracked dry gas according to claim 6, it is characterised in that：Diesel oil absorption tower（T2）
The absorption tower gaseous phase outlet at top（T2c）Pass through gas pipeline（G4）With gas ductwork（E3）It is connected.
9. the ethylene recovery system of catalytic cracked dry gas according to claim 4, it is characterised in that：The raw material surge tank
（V3）Outlet conduit on ethylene concentration survey meter is installed（S1）, the lean gas return valve（U1）Aperture be controlled by the second
Alkene concentration survey meter（S1）The ethylene concentration value detected.
10. the ethylene recovery system of catalytic cracked dry gas according to claim 5, it is characterised in that：Also include cooling tower
（T4）, the cooling tower（T4）It is connected with cooling tower upper hose（G7）With cooling tower downcomer（G8）；Cooling tower downcomer（G8）
Outlet and the 3rd cooler（L3）Cooling water inlet be connected, the 3rd cooler（L3）Coolant outlet and the preheater
（H4）Hot side import be connected, the preheater（H4）Hot side outlet and cooling water circulating pump（P6）Entrance be connected, it is described
Cooling water circulating pump（P6）Outlet and the cooling tower upper hose（G7）It is connected.
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| CN107739628A (en) * | 2017-11-01 | 2018-02-27 | 中国石油化工股份有限公司 | A kind of method by dilute ethylene recovery various ingredients |
| CN110452086A (en) * | 2019-08-30 | 2019-11-15 | 北京东方红升新能源应用技术研究院有限公司 | The recoverying and utilizing method of dry gas and application |
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