CN205607018U - System for utilize refinery dry gas - Google Patents
System for utilize refinery dry gas Download PDFInfo
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- CN205607018U CN205607018U CN201620321107.0U CN201620321107U CN205607018U CN 205607018 U CN205607018 U CN 205607018U CN 201620321107 U CN201620321107 U CN 201620321107U CN 205607018 U CN205607018 U CN 205607018U
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- azeotrope
- rectifying column
- gas
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- heat exchanger
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Abstract
The utility model discloses a system for utilize refinery dry gas, wherein, system for utilize refinery dry gas includes: one -level plate -fin heat exchanger, vapour and liquid separator, first rectifying column, second rectifying column, second grade plate -fin heat exchanger, third rectifying column, fourth rectifying column, a refrigerating system, the 2nd refrigerating system, the 3rd refrigerating system. The technical scheme of the utility model through the refrigerant that the adopts different warm areas refrigeration that circulates respectively to optimize multi -component separation sequence, thereby reach the effect of drawing, utilizing respectively each the component classification among the refinery dry gas, realize the make full use of of resource making investment and operating cost reduction simultaneously again as far as possible, improve economic nature.
Description
Technical field
This utility model relates to petrochemical industry, particularly relates to a kind of system utilizing oil refinery dry gas.
Background technology
Oil refinery dry gas refers to the noncondensable gas produced in oil refining process, is mainly derived from the secondary operations of crude oil
Process, such as RFCC, delayed coking etc., the dry gas amount that wherein catalytic cracking produces is most.Refinery
Dry gas complicated component, different process device produce dry gas composition also differ, mainly have ethylene, propylene,
Methane, ethane, propane, butane, hydrogen, nitrogen, carbon monoxide, carbon dioxide, possibly together with Determination of Trace Sulfur,
Mercury impurities.
Oil refinery dry gas uses usually used as fuel gas, even delivers to torch and directly burns.Along with technological progress and
The raising of people's understanding, everybody gradually recognizes that oil refinery dry gas recycles and produces into oil refining enterprise's reduction
This, to realize utilization of resources extremely important, relevant recovery development technique is continuously developed out.
Recycle currently, with respect to oil refinery dry gas and mainly have two kinds of thinkings.A kind of thinking is to take certain method
Ethylene that extraction and application certain several components, mainly economic worth therein are higher, propylene, hydrogen.This kind of
Method have cryogenic separation (patent 200410086381.6), cold oil absorption (patent 200910077780.9),
Adsorbing separation (patent 200810072849.4) and membrance separation (patent 201020504769.4 and patent 2014
20266803.7) and the group technology of multiple said method.But, said method only extracts or concentrates refining
Some components in factory's dry gas, the unrealized clear segmentation to component each in dry gas.Another thinking be by
Oil refinery dry gas uses directly as raw material, utilizes wherein useful constituent, as prepared dichloroethanes (patent
201110430297.1), propionic aldehyde (patent 201210132425.9), gasoline (patent 201110246922.7).
But each concentration of component in oil refinery dry gas is the highest, and containing the indifferent gas the most useless to lower procedure
Body, directly utilizes running cost of a relatively high, even affects the purity of downstream product.
Utility model content
The technical problems to be solved in the utility model is to provide a kind of can divide each component in oil refinery dry gas
The system utilizing oil refinery dry gas that class is extracted, is utilized respectively.
The system utilizing oil refinery dry gas of the present utility model, including:
For the one-level plate-fin heat exchanger that oil refinery dry gas cooling is processed；
For the oil refinery dry gas after cooling is carried out initial gross separation process, make the first liquid in described oil refinery dry gas
Stream and the gas-liquid separator of the first gas phase flow separation, be connected by pipeline with described one-level plate-fin heat exchanger mutually；
Make the first liquid phase stream isolate to include the of C2, C3 for the first liquid phase stream carries out essence separating treatment
Two liquid phase stream and the first rectifying column of the second gas phase stream, be connected by pipeline with described gas-liquid separator；
For second liquid phase stream being carried out the Second distillation column of essence separating treatment, pass through with described first rectifying column
Pipeline connects；
For two grades of plate-fin heat exchangers that the first gas phase stream, the second gas phase stream cooling are processed, with described gas-liquid
Separator and the first rectifying column are connected by pipeline；
For to cooling after the first gas phase stream, the second gas phase stream carry out essence separating treatment make the first gas phase stream,
Second gas phase flow point separates out the 3rd gas phase stream and the 3rd rectifying column of the 3rd liquid phase stream including hydrogen, with two
Level plate-fin heat exchanger is connected by pipeline；
Make the 3rd liquid phase stream isolate to include the 4th of nitrogen for the 3rd liquid phase stream carries out essence separating treatment
Gas phase stream and include the 4th rectifying column of the 4th liquid phase stream of methane, passes through pipeline with described 3rd rectifying column
Connect；
For providing the first refrigeration system of cold for the overhead condenser of Second distillation column,
For providing the second refrigeration system of cold for the overhead condenser of the first rectifying column,
For providing the of cold for the overhead condenser of the overhead condenser of the 3rd rectifying column, the 4th rectifying column
Three refrigeration systems.
The system utilizing oil refinery dry gas of the present utility model, wherein, the first refrigeration system is propane cycles refrigeration
System, described propane cycles refrigeration system include successively along propane flow direction the first propane compensator, for
To the propane compressor of propane compression of the first propane compensator output, the second propane compensator, for third
Alkane cooling heat exchanger, for propane throttling cooling first throttle valve, described heat exchanger pass through influent stream pipe
Road connects described first throttle valve, and the propane that described first throttle valve outlet port is communicated in described Second distillation column enters
Mouthful, the propane outlets of described Second distillation column is sequentially connected with described heat exchanger, the first propane by the pipeline that backflows
Compensator, so that propane is back to the first propane by the pipeline that backflows after providing cold in described Second distillation column
Compensator.
The system utilizing oil refinery dry gas of the present utility model, wherein, the second refrigeration system is azeotrope circulation
Refrigeration system, described azeotrope cycle refrigeration system includes the first mixing successively along azeotrope flow direction
Cryogen compensator, the azeotrope compression compressed for the azeotrope that the first azeotrope compensator is exported
Machine, the second azeotrope compensator, cooler, gas-liquid separator, the gas phase mixing of described gas-liquid separator
Cryogen outlet is by pipeline connection second throttle, and second throttle connects first by the first reflux pipe and mixes
Closing cryogen compensator, the liquid-phase mixing cryogen outlet of described gas-liquid separator is throttled by pipeline connection the 3rd
Valve, described 3rd choke valve is connected by the second reflux pipe and the first reflux pipe, so that by described second
Choke valve, the 3rd choke valve respectively throttle cooling after gas phase azeotrope, liquid-phase mixing cryogen converge after return
Flowing to the first azeotrope compensator, described azeotrope is put down at azeotrope compressor and the first azeotrope
Circulating between weighing apparatus tank, described first reflux pipe is through the first rectifying column, two grades of plate-fin heat exchangers, steps
Wing heat exchanger, the mixing in one-level plate-fin heat exchanger, the first reflux pipe of described second reflux pipe is cold
Agent provides cold, the second return duct in the first rectifying column, two grades of plate-fin heat exchangers, one-level plate-fin heat exchangers
Azeotrope in road provides cold in one-level plate-fin heat exchanger.
The system utilizing oil refinery dry gas of the present utility model, wherein, described 3rd refrigeration system is nitrogen circulation
Refrigeration system, described nitrogen circulation refrigeration system includes the first nitrogen balance successively along the flow direction of nitrogen
Tank, for first nitrogen balance tank output nitrogen compression nitrogen compressor, the second nitrogen balance tank,
Water cooler, water cooler is connected with one-level plate-fin heat exchanger, two grades of plate-fin heat exchangers successively by pipeline, described
Two grades of plate-fin heat exchangers are connected with the 4th choke valve for making nitrogen throttling lower the temperature by pipeline, and the described 4th
The outlet of choke valve is sequentially connected with the overhead condenser of the 4th rectifying column, the tower top of the 3rd rectifying column by pipeline
Condenser, the nitrogen outlet of the overhead condenser of the 3rd rectifying column is sequentially connected with described two by the 3rd reflux pipe
Level plate-fin heat exchanger, described one-level plate-fin heat exchanger, the first nitrogen balance tank, so that nitrogen is the described 4th
The overhead condenser of rectifying column, the 3rd rectifying column overhead condenser in provide after cold by the 3rd reflux pipe
It is back to the first nitrogen balance after sequentially passing through described two grades of plate-fin heat exchangers, described one-level plate-fin heat exchanger
Tank.
The technical solution of the utility model is by using the cold-producing medium circularly cooling respectively of different warm area, and optimizes
Multi-component separation sequence, thus reach the effect each constituent classification in oil refinery dry gas extracted, is utilized respectively
Really, it is achieved making full use of of resource, make investment and operating cost reduce simultaneously the most as far as possible, improve economy.
Accompanying drawing explanation
Fig. 1 is the structural representation of the system utilizing oil refinery dry gas of the present utility model.
Detailed description of the invention
As it is shown in figure 1, the system utilizing oil refinery dry gas of the present utility model, including:
For the one-level plate-fin heat exchanger 121 that oil refinery dry gas cooling is processed；
For the oil refinery dry gas after cooling is carried out initial gross separation process, make the first liquid in described oil refinery dry gas
Stream and the gas-liquid separator 131 of the first gas phase flow separation, connected by pipeline with described one-level plate-fin heat exchanger mutually
Connect；
Make the first liquid phase stream isolate to include the of C2, C3 for the first liquid phase stream carries out essence separating treatment
Two liquid phase stream and the first rectifying column 141 of the second gas phase stream, with described gas-liquid separator by pipeline even
Connect；
For second liquid phase stream being carried out the Second distillation column 142 of essence separating treatment, with described first rectifying column
Connected by pipeline；
For two grades of plate-fin heat exchangers 122 that the first gas phase stream, the second gas phase stream cooling are processed, with described
Gas-liquid separator and the first rectifying column are connected by pipeline；
For to cooling after the first gas phase stream, the second gas phase stream carry out essence separating treatment make the first gas phase stream,
Second gas phase flow point separates out the 3rd gas phase stream and the 3rd rectifying column 143 of the 3rd liquid phase stream including hydrogen,
It is connected by pipeline with two grades of plate-fin heat exchangers；
Make the 3rd liquid phase stream isolate to include the 4th of nitrogen for the 3rd liquid phase stream carries out essence separating treatment
Gas phase stream and include the 4th rectifying column 144 of the 4th liquid phase stream of methane, passes through with described 3rd rectifying column
Pipeline connects；
For providing the first refrigeration system of cold for the overhead condenser of Second distillation column,
For providing the second refrigeration system of cold for the overhead condenser of the first rectifying column,
For providing the of cold for the overhead condenser of the overhead condenser of the 3rd rectifying column, the 4th rectifying column
Three refrigeration systems.
The system utilizing oil refinery dry gas of the present utility model, wherein, the first refrigeration system is propane cycles refrigeration
System 151, described propane cycles refrigeration system include successively along propane flow direction the first propane compensator,
For the propane compressor of propane compression, the second propane compensator that the first propane compensator is exported, it is used for
To the heat exchanger of propane-cooled, for the first throttle valve to propane throttling cooling, described heat exchanger pass through into
First throttle valve described in stream pipeline connection, described first throttle valve outlet port is communicated in the third of described Second distillation column
Alkane entrance, the propane outlets of described Second distillation column by the pipeline that backflows be sequentially connected with described heat exchanger, first
Propane compensator, so that propane is back to first by the pipeline that backflows after providing cold in described Second distillation column
Propane compensator.
The system utilizing oil refinery dry gas of the present utility model, wherein, the second refrigeration system is azeotrope circulation
Refrigeration system 152, described azeotrope cycle refrigeration system includes first successively along azeotrope flow direction
Azeotrope compensator, the azeotrope compressed for the azeotrope that the first azeotrope compensator is exported
Compressor, the second azeotrope compensator, cooler, gas-liquid separator, the gas phase of described gas-liquid separator
Azeotrope outlet is by pipeline connection second throttle, and second throttle connects the by the first reflux pipe
One azeotrope compensator, the liquid-phase mixing cryogen of described gas-liquid separator exports by pipeline connection Section three
Stream valve, described 3rd choke valve is by the connection of the second reflux pipe and the first reflux pipe, so that by described the
Two choke valves, the 3rd choke valve throttle respectively the gas phase azeotrope after cooling, after liquid-phase mixing cryogen converges
Being back to the first azeotrope compensator, described azeotrope is at azeotrope compressor and the first azeotrope
Circulating between compensator, described first reflux pipe is through the first rectifying column, two grades of plate-fin heat exchangers, one-levels
Plate-fin heat exchanger, the mixing in one-level plate-fin heat exchanger, the first reflux pipe of described second reflux pipe
Cryogen provides cold, the second backflow in the first rectifying column, two grades of plate-fin heat exchangers, one-level plate-fin heat exchangers
Azeotrope in pipeline provides cold in one-level plate-fin heat exchanger.
The system utilizing oil refinery dry gas of the present utility model, wherein, described 3rd refrigeration system is nitrogen circulation
Refrigeration system 153, along the flow direction of nitrogen, described nitrogen circulation refrigeration system includes that the first nitrogen is put down successively
Weighing apparatus tank, for first nitrogen balance tank output nitrogen compression nitrogen compressor, the second nitrogen balance tank,
Water cooler, water cooler is connected with one-level plate-fin heat exchanger, two grades of plate-fin heat exchangers successively by pipeline, described
Two grades of plate-fin heat exchangers are connected with the 4th choke valve for making nitrogen throttling lower the temperature by pipeline, and the described 4th
The outlet of choke valve is sequentially connected with the overhead condenser of the 4th rectifying column, the tower top of the 3rd rectifying column by pipeline
Condenser, the nitrogen outlet of the overhead condenser of the 3rd rectifying column is sequentially connected with described two by the 3rd reflux pipe
Level plate-fin heat exchanger, described one-level plate-fin heat exchanger, the first nitrogen balance tank, so that nitrogen is the described 4th
The overhead condenser of rectifying column, the 3rd rectifying column overhead condenser in provide after cold by the 3rd reflux pipe
It is back to the first nitrogen balance after sequentially passing through described two grades of plate-fin heat exchangers, described one-level plate-fin heat exchanger
Tank.
Nitrogen circulates between nitrogen compressor and the first nitrogen balance tank.
The system utilizing oil refinery dry gas of the present utility model, including three grades of cycle refrigeration systems, i.e. propane cycles
Refrigeration system, azeotrope cycle refrigeration system, nitrogen circulation refrigeration system.Three grades of cycle refrigeration systems divide
Do not provide cold at different warm areas for oil refinery dry gas separation process, be respectively propane according to potential temperature from high to low and follow
Ring refrigeration system, azeotrope cycle refrigeration system and nitrogen circulation refrigeration system.
The technical solution of the utility model is by optimizing separation sequence and the appropriate design of multistage refrigerating plant, real
Showed the clear segmentation of each component in oil refinery dry gas, produce respectively LNG (methane), hydrogen rich gas, C2 and
Tetra-products of C3+, are respectively used to different purposes, it is achieved in oil refinery dry gas, each component is effective by each product
Utilize, maximization of economic benefit.
Active component methane content about 15～50% in oil refinery dry gas, hydrogen content about 20～30%, C2 content
About 15～25%, C3+ content about 1～3%, additionally contain the noble gases such as a small amount of carbon monoxide, nitrogen with
And the organic sulfur of carbon dioxide, trace, SO2, dust, the impurity such as steam.
The overhead condenser that propane cycles refrigeration system is Second distillation column provides cold, and residing warm area is room temperature
～-30 DEG C.
Azeotrope cycle refrigeration system is the overhead condenser of the first rectifying column and unstripped gas is cooled to
-130～-165 DEG C of processes colds are provided, residing warm area is room temperature～-165 DEG C.
Nitrogen circulation refrigeration system is the overhead condenser of the 3rd rectifying column, the overhead condenser of the 4th rectifying column
And unstripped gas is cooled to-130～165 DEG C of processes and provides colds, residing warm area is room temperature～-185 DEG C.
The system utilizing oil refinery dry gas of the present utility model, wherein, the gas-liquid of azeotrope cycle refrigeration system
The gas phase azeotrope outlet of separator connects second throttle by air inlet pipeline, and air inlet pipeline is through the 4th
The tower reactor of rectifying column, the tower reactor institute calorific requirement of the 4th rectifying column is from the gas phase azeotrope in air inlet pipeline.
The technical solution of the utility model is utilized to carry out utilizing the enforcement of oil refinery dry gas to include two flow processs:
1, unstripped gas flow process
Oil refinery dry gas after purified, dried, first transporting enter one-level plate-fin heat exchanger cool to
-90～-120 DEG C, then it is respectively adopted a gas-liquid separation and a rectification processes, isolated gas phase
And liquid phase stream, wherein liquid phase stream uses a rectification process again, obtains the liquid phase based on C2, C3
Product, obtains the product based on C2 after liquid-phase product rectification process and C3 is main product, and C2 is main
Product rewarming after deliver to ethylbenzene production process, the product that C3 is main delivers to LPG storage tank.At rectification
The gaseous stream that obtains of reason is fed again into plate-fin heat exchanger and is cooled to-130～-165 DEG C further, then carries out
Rectification process, rectifying column tower top obtains the hydrogen rich gas product based on hydrogen, after hydrogen rich gas product rewarming
Delivering to PSA and put forward hydrogen operation, tower bottom liquid phase logistics carries out a rectification process the most again, and rectifying column tower top obtains
Tail gas based on nitrogen, then obtains LNG product, delivers to LNG storage tank at the bottom of tower.
2, compression circularly cooling flow process
Owing to the complicated components of oil refinery dry gas, each constituent content are relatively average, in order to realize each constituent classification
The target purified, uses a set of cycle refrigeration system energy consumption relatively big, for this according to potential temperature needed for each Component seperation
Difference, design three set cycle refrigeration systems realize above-mentioned target, the most also can be effectively reduced operation energy consumption.
According to potential temperature height, three set circularly cooling techniques are followed successively by propane cycles refrigeration system, azeotrope circularly cooling
System and nitrogen circulation refrigeration system.
(1) propane cycles refrigeration system
The Main Function of propane cycles refrigeration system is the separation offer cold for C2 and C3, is the second essence
The overhead condenser evaporating tower provides cold.
Refrigerative circle system is as follows: after propane first passes through low-pressure balance tank buffering, enter propane compressor entrance,
Pressure raise after after heat exchanger is cooled to 30 DEG C throttling refrigeration, the overhead condenser for Second distillation column carries
Semen donors, after being then back to heat exchanger rewarming, enters low-pressure balance tank, completes whole kind of refrigeration cycle.
(2) azeotrope cycle refrigeration system
The Main Function of azeotrope cycle refrigeration system is that the initial gross separation of unstripped gas provides cold (to comprise
CH4Separate with C2+ component in interior light component), the overhead condenser being the first rectifying column provides cold,
Unstripped gas is cooled to-130～-165 DEG C simultaneously in advance, and the separation for light component provides advantage.
Azeotrope mixed according to a certain percentage by materials such as nitrogen, methane, ethylene, propane, isopentane and
Becoming, refrigerative circle system is as follows: the azeotrope of low pressure enters cooling after entering azeotrope compressor boost
Device, enters gas-liquid separator after being cooled to 40 DEG C, isolated liquid phase delivers to one-level plate-fin heat exchanger, cold
But, after throttling, then backflow rewarming cooling box；Isolated gas phase sequentially pass through one-level plate-fin heat exchanger, two
Throttling refrigeration after level plate-fin heat exchanger, finally backflow rewarming, backflows with liquid phase and blends ice chest, returns to mixing
Refrigerant compressor entrance, completes whole kind of refrigeration cycle.
(3) nitrogen circulation refrigeration system
The main purpose of nitrogen circulation refrigeration system is as low boiling component (methane, hydrogen, nitrogen)
Separate and cold is provided, the overhead condenser offer cold of the 3rd rectifying column, the 4th rectifying column, its temperature are provided
It is reduced to-170～-180 DEG C.Also work during unstripped gas is cooled to-130～-165 DEG C simultaneously, for
The separation of light component provides advantage.
Refrigerative circle system is as follows: after nitrogen cryogen first passes through nitrogen balance tank surge tank, enters nitrogen compression
Machine entrance, pressure is cooled to 40 DEG C through water cooler after raising and enters ice chest, sequentially passes through a step wing heat exchange
Throttling refrigeration after device, two grades of plate-fin heat exchangers, is that the overhead condenser of the 3rd rectifying column and the 4th rectifying column carries
Semen donors, after being then back to heat exchanger rewarming, enters nitrogen balance tank, completes whole kind of refrigeration cycle.
As shown in table 1, pressure is 0.7MPa (G) to typical refinery dry gas composition, and temperature is about 40 DEG C, stream
Amount is 20000Nm3/h。
Table 1 feed gas composition and content
As it is shown in figure 1, the unstripped gas (stream stock 1) after purified dried sends into one-level plate-fin heat exchanger
121 are cooled to-90～-120 DEG C, send into gas-liquid separator 131 and carry out initial gross separation, gained liquid phase stream stock 3
Sending into the first rectifying column 141 and carry out essence separation, gained gas phase stream stock 6 and stream stock 4 merge into stream stock 7 and send into
Two grades of plate-fin heat exchangers 122 are lowered the temperature further.In first rectifying column 141 gained liquid phase stream stock 5 mainly by
C2, C3+ form, and are re-fed into Second distillation column 142 and carry out essence separation, and tower top obtains the product based on C2
Product deliver to ethylbenzene production process (stream stock 10) after returning one-level plate-fin heat exchanger 121 rewarming, obtain at the bottom of tower
C3+ product (stream stock 9) delivers to LPG storage tank.Stream stock 7 key component be hydrogen, nitrogen, methane,
The light component such as carbon monoxide, separates needs cooling further to realize three, delivers to two grades of plate-fin heat exchangers
122 are cooled to-130～-165 DEG C, are then sent to the 3rd rectifying column 143 and carry out essence separation, overwhelming majority hydrogen
And a small amount of nitrogen, carbon monoxide are from overhead extraction (stream stock 12), sequentially pass through two grades of plate-fin heat exchangers 122,
Delivering to PSA after one-level plate-fin heat exchanger 121 rewarming and put forward hydrogen operation (stream stock 17), tower bottom liquid flows stock 13 mutually
Then deliver to the 4th rectifying column 144 essence further separate, overwhelming majority nitrogen and a small amount of hydrogen, carbon monoxide from
Overhead extraction (stream stock 15), sequentially passes through two grades of plate-fin heat exchangers 122, one-level plate-fin heat exchanger 121 again
Send battery limit (BL) (stream stock 19) after temperature, at the bottom of tower, obtain the liquid form product (stream stock 14) rich in methane.
In Fig. 1,151 is propane cycles refrigeration system, and 152 is azeotrope cycle refrigeration system, 153
For nitrogen circulation refrigeration system.
Table 2 product forms
| Stream stock | 10 | 9 | 14 | 17 | 19 |
| CH4 | 1.29 | 0.00 | 94.05 | 0.79 | 1.00 |
| C2H6 | 63.94 | 9.06 | 2.03 | 0.00 | 0.00 |
| C3H8 | 0.00 | 31.47 | 0.00 | 0.00 | 0.00 |
| C2H4 | 34.75 | 0.00 | 3.61 | 0.00 | 0.00 |
| C4+ | 0.00 | 33.18 | 0.00 | 0.00 | 0.00 |
| H2 | 0.00 | 0.00 | 0.00 | 74.31 | 8.69 |
| CO | 0.00 | 0.00 | 0.20 | 3.17 | 16.31 |
| N2 | 0.00 | 0.00 | 0.10 | 21.73 | 74.00 |
| C3H6 | 0.01 | 26.28 | 0.01 | 0.00 | 0.00 |
| Flow Nm3/h | 3685 | 305 | 6873 | 7331 | 1357 |
| Pressure MPa (G) | 1.4 | 1.5 | 0.015 | 1.4 | 0.5 |
| Temperature DEG C | 30 | 40 | -161 | 30 | 30 |
The refinery dry gas of complicated component through a series of purification separation process after, obtain hydrogen rich gas, LNG,
The products such as C2, C3+, its composition is shown in Table 2, and wherein hydrogen rich gas is sent to PSA and puies forward hydrogen operation, and C2 product send
Toward ethylbenzene production process, C3+ product is as commodity export trade, it is achieved that the rational and efficient use of resource, its warp
Ji property significantly improves.
Below it is only preferred implementation of the present utility model, it is noted that common for the art
For technical staff, on the premise of without departing from this utility model principle, it is also possible to make some improvement and profit
Decorations, these improvements and modifications also should be regarded as protection domain of the present utility model.
Claims (4)
1. the system utilizing oil refinery dry gas, it is characterised in that including:
For the one-level plate-fin heat exchanger that oil refinery dry gas cooling is processed；
For the oil refinery dry gas after cooling is carried out initial gross separation process, make the first liquid in described oil refinery dry gas
Stream and the gas-liquid separator of the first gas phase flow separation, be connected by pipeline with described one-level plate-fin heat exchanger mutually；
Make the first liquid phase stream isolate to include the of C2, C3 for the first liquid phase stream carries out essence separating treatment
Two liquid phase stream and the first rectifying column of the second gas phase stream, be connected by pipeline with described gas-liquid separator；
For second liquid phase stream being carried out the Second distillation column of essence separating treatment, pass through with described first rectifying column
Pipeline connects；
For two grades of plate-fin heat exchangers that the first gas phase stream, the second gas phase stream cooling are processed, with described gas-liquid
Separator and the first rectifying column are connected by pipeline；
For to cooling after the first gas phase stream, the second gas phase stream carry out essence separating treatment make the first gas phase stream,
Second gas phase flow point separates out the 3rd gas phase stream and the 3rd rectifying column of the 3rd liquid phase stream including hydrogen, with two
Level plate-fin heat exchanger is connected by pipeline；
Make the 3rd liquid phase stream isolate to include the 4th of nitrogen for the 3rd liquid phase stream carries out essence separating treatment
Gas phase stream and include the 4th rectifying column of the 4th liquid phase stream of methane, passes through pipeline with described 3rd rectifying column
Connect；
For providing the first refrigeration system of cold for the overhead condenser of Second distillation column,
For providing the second refrigeration system of cold for the overhead condenser of the first rectifying column,
For providing the of cold for the overhead condenser of the overhead condenser of the 3rd rectifying column, the 4th rectifying column
Three refrigeration systems.
Utilize the system of oil refinery dry gas the most as claimed in claim 1, it is characterised in that the first refrigeration system
System is propane cycles refrigeration system, and described propane cycles refrigeration system includes first successively along propane flow direction
Propane compensator, the propane compressor of propane compression for the first propane compensator is exported, the second propane
Compensator, for the heat exchanger of propane-cooled, for the first throttle valve to propane throttling cooling, described
Heat exchanger is by first throttle valve described in influent stream pipeline connection, and described first throttle valve outlet port is communicated in described the
The propane inlet of two rectifying columns, the propane outlets of described Second distillation column is sequentially connected with described by the pipeline that backflows
Heat exchanger, the first propane compensator, so that propane provides after cold by return tube in described Second distillation column
Road is back to the first propane compensator.
Utilize the system of oil refinery dry gas the most as claimed in claim 2, it is characterised in that the second refrigeration system
System is azeotrope cycle refrigeration system, and described azeotrope cycle refrigeration system is along azeotrope flow direction
Include the first azeotrope compensator successively, for the azeotrope pressure to the first azeotrope compensator output
The azeotrope compressor of contracting, the second azeotrope compensator, cooler, gas-liquid separator, described gas-liquid
The gas phase azeotrope outlet of separator is passed through first time by pipeline connection second throttle, second throttle
Flow tube road connects the first azeotrope compensator, and the liquid-phase mixing cryogen outlet of described gas-liquid separator is by pipe
Road connection the 3rd choke valve, described 3rd choke valve is connected by the second reflux pipe and the first reflux pipe,
So that being throttled respectively by described second throttle, the 3rd choke valve, the gas phase azeotrope after lowering the temperature, liquid phase are mixed
Close cryogen converge after be back to the first azeotrope compensator, described azeotrope azeotrope compressor with
Circulating between first azeotrope compensator, described first reflux pipe is through the first rectifying column, two step wings
Heat exchanger, one-level plate-fin heat exchanger, described second reflux pipe is through one-level plate-fin heat exchanger, the first backflow
Azeotrope in pipeline provides cold in the first rectifying column, two grades of plate-fin heat exchangers, one-level plate-fin heat exchangers
Amount, the azeotrope in the second reflux pipe provides cold in one-level plate-fin heat exchanger.
Utilize the system of oil refinery dry gas the most as claimed in claim 3, it is characterised in that described 3rd system
Cooling system is nitrogen circulation refrigeration system, described nitrogen circulation refrigeration system along nitrogen flow direction successively
Including the first nitrogen balance tank, for first nitrogen balance tank output nitrogen compression nitrogen compressor,
Second nitrogen balance tank, water cooler, water cooler by pipeline successively with one-level plate-fin heat exchanger, two step wings
Heat exchanger connects, and described two grades of plate-fin heat exchangers are by pipeline and the 4th throttling for making nitrogen throttling cooling
Valve connect, described 4th choke valve outlet by pipeline be sequentially connected with the 4th rectifying column overhead condenser,
The overhead condenser of the 3rd rectifying column, the nitrogen of the overhead condenser of the 3rd rectifying column exports by the 3rd return duct
Road is sequentially connected with described two grades of plate-fin heat exchangers, described one-level plate-fin heat exchanger, the first nitrogen balance tank, with
Nitrogen is made to provide cold in the described overhead condenser of the 4th rectifying column, the overhead condenser of the 3rd rectifying column
After sequentially passed through by the 3rd reflux pipe and to reflux after described two grades of plate-fin heat exchangers, described one-level plate-fin heat exchanger
To the first nitrogen balance tank.
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| CN201620321107.0U CN205607018U (en) | 2016-04-15 | 2016-04-15 | System for utilize refinery dry gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105737518A (en) * | 2016-04-15 | 2016-07-06 | 北京中科瑞奥能源科技股份有限公司 | System and method utilizing refinery dry gas |
| CN115253612A (en) * | 2022-08-25 | 2022-11-01 | 国家能源集团宁夏煤业有限责任公司 | Fischer-Tropsch synthesis tail gas separation and recovery system and method |
-
2016
- 2016-04-15 CN CN201620321107.0U patent/CN205607018U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105737518A (en) * | 2016-04-15 | 2016-07-06 | 北京中科瑞奥能源科技股份有限公司 | System and method utilizing refinery dry gas |
| CN115253612A (en) * | 2022-08-25 | 2022-11-01 | 国家能源集团宁夏煤业有限责任公司 | Fischer-Tropsch synthesis tail gas separation and recovery system and method |
| CN115253612B (en) * | 2022-08-25 | 2024-02-02 | 国家能源集团宁夏煤业有限责任公司 | Fischer-Tropsch synthesis tail gas separation and recovery system and method |
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Granted publication date: 20160928 Effective date of abandoning: 20171205 |