CN110330018A - It is a kind of to prepare dry ice using LNG cold energy and separate the device and working method of ethylene - Google Patents
It is a kind of to prepare dry ice using LNG cold energy and separate the device and working method of ethylene Download PDFInfo
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- CN110330018A CN110330018A CN201910444287.XA CN201910444287A CN110330018A CN 110330018 A CN110330018 A CN 110330018A CN 201910444287 A CN201910444287 A CN 201910444287A CN 110330018 A CN110330018 A CN 110330018A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
- C01B32/55—Solidifying
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of devices and working method that dry ice and separation ethylene are prepared using LNG cold energy, and described device includes: ethylene refining system and dry ice manufacture system.LNG cold energy is shunted by triple valve, the second heat exchanger and First Heat Exchanger for sequentially entering ethylene refining system all the way for ethylene refining system provide depth cooling capacity, another way with from First Heat Exchanger come out LNG cold energy converge after enter carbon dioxide ice maker, LNG after vaporization heating is passed through gas turbine for gas turbine power generation, realizes the cascade utilization of LNG cold energy.Cracking gas enters ethylene refining system and goes out one component of carbon, hydrogen-rich gas, two component of carbon and heavier component using LNG cooling capacity and the differential separation according to component weight, and ethylene finally is made using acetylene hydrogenation device.The present invention realizes inexpensive ethylene purification and dry ice manufacture function.
Description
Technical field
The present invention relates to a kind of devices and working method that dry ice and separation ethylene are prepared using LNG cold energy, pass through dry ice
Organic cooperation of manufacture system and ethylene refining system has also reached zero carbon emission of manufacture dry ice while realizing ethylene purification
Requirement.Belong to field of energy utilization.
Background technique
In recent years, with the fast development of Gas Industry, High-efficiency Gas utilizes and has become research hotspot.Due to coal
The burning of petroleum causes irremediable destruction to atmosphere, so application of the natural gas in every field has become following hair
Exhibition trend.This system needs to consume under the background of mass energy based on chemical plant, is chemical plant manufacture using the cold energy of LNG release
Basic chemical raw materials ethylene, while dry ice is manufactured by raw material of the byproduct carbon dioxide in chemical plant, both obtained income or reality
Show zero carbon emission, protects environment.It largely realizes energy-saving and emission-reduction, simultaneously for environmental protection there is great reality to anticipate
Justice.
LNG is a kind of -160.0 DEG C of cryogenic liquid under normal pressure, needs to be gasified before being supplied to downstream user and add
Heat usually realized using seawater or fuel to 0 DEG C or more, and when LNG vaporization can release a large amount of cold energy, causes the very big of the energy
Waste.According to current LNG production technology, power consumption is about 850kWh/t (in terms of LNG per ton), and is receiving terminal
1.0t LNG vaporization about can release the cold energy of about 230kWh.Using LNG as each process-stream in cold source, cracking gas separation
For cold-trap, carry out substituting refrigeration duty needed for three machine compression refrigerating systems provide ethylene deep cooling process for separating with LNG cooling capacity part
Research, can reduce the energy consumption of LNG gasification cost and ethylene cryogenic separation.
In the prior art, the Chinese patent of 103542693 A of Publication No. CN proposes a kind of for large-scale ethylene plant
Ethylene deep cooling separating method, this method is provided with three coolers and two expansions-recompression machine to recycle cooling capacity be system
Cooling supply, and cooler and expansion-recompression machine need to consume a large amount of electric energy, increase the energy consumption of system.And the present invention utilizes LNG
Cooling supply is vaporized, does not need to set up cooler and expansion-recompression machine, it is only necessary to set up heat exchanger, be generated using LNG vaporization cold
Measure supplying cold directly, result of study show utilization rate of the LNG cold energy in ethylene separation technique up to 76.5%, every 300,000 tons of production
The cooling capacity load of about 22000kW in the alternative original process of ethylene saves the cryogen compression refrigerating system power consumption of about 20000kW, greatly
The energy consumption cost of amplitude reduction ethylene cryogenic separation device is single to be used to prepare ethylene and reach since LNG vaporization cold energy is huge
To the best available utilization of resource, therefore the present invention system of dry ice manufacture in parallel, LNG cold energy is not only taken full advantage of,
Also achieve zero carbon emission in chemical plant.
Summary of the invention
It is an object of the invention to overcome the deficiencies in the prior art, so provide it is a kind of using LNG cold energy prepare dry ice and
Separate the device and working method of ethylene.
The present invention is to realize chemical plant base stock second by the way that dry ice manufacture system and ethylene refining system are coupled
The low cost purification of alkene, while the byproduct carbon dioxide in chemical plant is subjected to capture using LNG cold energy, dry ice is made, it is neither unrestrained
Expense LNG cooling capacity provides income again for chemical plant, also protects environment, the economy and environmental protection that the system that improves integrally is runed
Property.
In order to achieve the above objectives, the present invention adopts the following technical scheme:
It is a kind of to prepare dry ice using LNG cold energy and separate the device of ethylene, including dry ice manufacture system and ethylene purification system
System two parts, wherein the dry ice manufacture system includes: LNG pump, triple valve, carbon dioxide ice maker, gas turbine, generator, height
Carbon dioxide air accumulator, dry ice incubator are pressed, the LNG pump connects the right interface of the triple valve, the triple valve by pipeline
Left interface connects carbon dioxide ice maker bottom right interface by pipeline, and the high-pressure carbon dioxide reservoir outlet is connected by pipeline
The carbon dioxide ice maker entrance is connect, the carbon dioxide ice maker outlet connects the dry ice incubator, the dry ice system by pipeline
It makes machine upper right interface and the gas turbine is connected by pipeline, the gas turbine is connected by axis with the generator；It is described
Ethylene refining system includes: to crack gas tank First Heat Exchanger, the first precut tower, the second heat exchanger, gas-liquid separator, acetylene to add
Hydrogen production device, domethanizing column, ethylene tank, dethanizer, carbon three and more heavy constituent outlet, the cracking gas tank are connected by pipeline
First Heat Exchanger lower-left interface, First Heat Exchanger bottom right interface connect a described first precut tower left side by pipeline and connect
Mouthful, interface connects second heat exchanger lower-left interface by pipeline on the first precut tower, and second heat exchanger is right
Lower interface connects the left interface of the gas-liquid separator by pipeline, and interface connects the second by pipeline on the gas-liquid separator
Interface on alkynes hydrogenation plant, the right interface of acetylene hydrogenation device connect the ethylene tank, the gas-liquid separator by pipeline
Lower interface connects the left interface of the domethanizing column by pipeline, and the domethanizing column lower interface connects the deethanization by pipeline
The left interface of tower, the triple valve lower interface connect the second heat exchanger upper right interface by pipeline, and second heat exchanger is left
Upper interface connects the First Heat Exchanger upper right interface by pipeline, and First Heat Exchanger upper left interface connects institute by pipeline
Carbon dioxide ice maker bottom right interface is stated, the first precut tower lower interface connects the left interface of the dethanizer, institute by pipeline
It states dethanizer lower interface and the carbon three and more heavy constituent outlet is connected by pipeline, interface passes through pipeline in the ethane tower
Connect acetylene hydrogenation device lower interface.
Further, the demethanation process of the domethanizing column uses high-pressure process or low-pressure process.
Further, regulating valve is equipped between the high-pressure carbon dioxide air accumulator and the carbon dioxide ice maker.
Further, catalyst is equipped in the acetylene hydrogenation device, the catalyst is palladium or palladium-silver.
Further, the second precut tower is equipped between the described first precut tower and the dethanizer, described second is pre-
Cutting Tap connects the carbon three and more heavy constituent outlet by pipeline.
Further, the First Heat Exchanger and second heat exchanger are pipe heat exchanger or plate-fin heat exchanger.
It is a kind of to prepare dry ice using LNG cold energy and separate the working method of the device of ethylene are as follows:
(a) LNG is divided into two-way through the LNG pump and the triple valve, sequentially enters second heat exchanger and institute all the way
State First Heat Exchanger vaporization released cold quantity, another way with from the First Heat Exchanger come out LNG converge after enter the dry ice
Manufacturing machine, the regulating valve enter the carbon dioxide amount of the carbon dioxide ice maker, gas phase dioxy according to the cooling capacity control of LNG
Change carbon absorbs LNG cooling capacity in the carbon dioxide ice maker and produces dry ice, and finished product dry ice is gone out by the dry ice of the carbon dioxide ice maker
Mouth, which enters in the dry ice incubator, to be stored, and the LNG after vaporization heating is passed through the gas turbine for the electrical power generators；
(b) cracking gas enters the described first precut tower after First Heat Exchanger pre-cooling and is separated, carbon one and more
Light component and two component of a small amount of carbon are in a gaseous form from the described first precut column overhead outflow, into second heat exchanger
Cryogenic separation, carbon one of the boiling point lower than -162 DEG C and two component of carbon are liquefied, the hydrogen and a small amount of indifferent gas that boiling point is -252 DEG C
Body is still gaseous state, and the subsequent gas-liquid mixture enters the gas-liquid separator and carries out gas-liquid separation, and hydrogen-rich gas is passed through the second
Alkynes hydrogenation plant provides necessary hydrogen preparing ethylene for the acetylene hydrogenation device, and the carbon one and two component of carbon being liquefied are by institute
The lower outlet for stating gas-liquid separator enters the domethanizing column, and one component of carbon flows out by the demethanizer column overhead, carbon two and more
Heavy constituent enters the dethanizer by tower bottom, and a large amount of carbon two of the first precut tower separation and more heavy constituent are by described the
The tower bottom of one precut tower enters the described second precut tower, the carbon two isolated through the described second precut tower and more light component
And a small amount of three component of carbon enters the dethanizer, the carbon that the dethanizer is isolated by the tower top of the described second precut tower
Two components enter the acetylene hydrogenation device by tower top, and two component of carbon and hydrogen-rich gas generate ethylene under the effect of the catalyst,
It stores to the ethylene tank, carbon three and more heavy constituent are flowed out by the tower bottom of the dethanizer and the second precut tower, most
It is discharged eventually by the carbon three and more heavy constituent outlet.
Compared with the prior art, the present invention has the following advantages and the utility model has the advantages that
1, this system is considered to utilize chemical plant LNG resource itself, does not need to set up expansion-recompression machine, every production 30
Ten thousand tons of ethylene about save the cryogen compression refrigerating system power consumption of 20000kW, reduce the cost in chemical plant.
2, the present invention has recycled a large amount of cold energy of LNG vaporization generation, and about 830-860kJ/kg is basic for separating chemical industry
Feed ethylene, therefore chemical plant does not need additionally to buy ethylene, and cooling capacity is avoided directly to be taken away by seawater, reduce the wave of the energy
Take.
3, all C-2-fractions all enter dethanizer in existing invention, and the tower load is caused to reach the 140% of design value,
The average only 681t/d of ethylene yield.Therefore the present invention is provided with the second precut tower between the first precut tower and dethanizer,
It avoids cracking gas component from laying particular stress on the load for increasing dethanizer, also improves the production efficiency of ethylene, about can reach 720t/d.
4, the basic component devices that ethylene is prepared in existing invention are 19, and the present invention only needs 13 to can reach accordingly
Purpose simultaneously improves yield, reduces the complexity of system.
5, utilization rate of the LNG cooling capacity in ethylene cryogenic separation is about 75%, therefore this patent dry ice manufacture in parallel
System, utilization rate not only can achieve 80% or more, also achieve zero carbon emission in chemical plant.
Detailed description of the invention
Fig. 1, which is that the present invention is a kind of, to be prepared dry ice using LNG cold energy and separates the principle schematic diagram of the device of ethylene；
In figure: 1 being cracking gas tank, 2 be First Heat Exchanger, 3 be the first precut tower, 4 be the second heat exchanger, 5 be gas-liquid
Separator, 6 be acetylene hydrogenation device, 7 be domethanizing column, 8 be ethylene tank, 9 be dethanizer, 10 be the second precut tower, 11
It is LNG pump for carbon three and more heavy constituent outlet, 12,13 be triple valve, 14 be carbon dioxide ice maker, 15 be gas turbine, 16 is
Generator, 17 be high-pressure carbon dioxide air accumulator, 18 be regulating valve, 19 be dry ice incubator.
Specific embodiment
To keep above-mentioned purpose of the invention, characteristics and advantages more obvious and easy to understand, with reference to the accompanying drawing to tool of the invention
Body applies example and elaborates.
As shown in Figure 1, for a kind of device for preparing dry ice and separation ethylene using LNG cold energy of the embodiment of the present invention, packet
Include dry ice manufacture system and ethylene refining system two parts, wherein the dry ice manufacture system include: LNG pump 12, triple valve 13,
Carbon dioxide ice maker 14, gas turbine 15, generator 16, high-pressure carbon dioxide air accumulator 17, regulating valve 18, dry ice incubator 19,
The LNG pump 12 connects the right interface of the triple valve 13 by pipeline, and the left interface of the triple valve 13 passes through described in pipeline connection
14 bottom right interface of carbon dioxide ice maker, the outlet of high-pressure carbon dioxide air accumulator 17 connect 18 left side of regulating valve by pipeline and connect
Mouthful, the right interface of the regulating valve 18 connects 14 entrance of carbon dioxide ice maker by pipeline, and the outlet of carbon dioxide ice maker 14 is logical
Piping connects the dry ice incubator 19, and the 14 upper right interface of carbon dioxide ice maker connects the gas turbine by pipeline
15, the gas turbine 15 is connected by axis with the generator 16；The ethylene refining system includes: cracking gas tank 1, first
Heat exchanger 2, the first precut tower 3, the second heat exchanger 4, gas-liquid separator 5, acetylene hydrogenation device 6, domethanizing column 7, ethylene tank
8, dethanizer 9, the second precut tower 10, carbon three and more heavy constituent outlet 11, the cracking gas tank 1 connect institute by pipeline
2 lower-left interface of First Heat Exchanger is stated, the 2 bottom right interface of First Heat Exchanger connects described first precut 3 left side of tower by pipeline
Interface, interface connects the 4 lower-left interface of the second heat exchanger, second heat exchange by pipeline on the first precut tower 3
4 bottom right interface of device connects the left interface of the gas-liquid separator 5 by pipeline, and interface is connected by pipeline on the gas-liquid separator 5
Interface on the acetylene hydrogenation device 6 is connect, the right interface of the acetylene hydrogenation device 6 connects the ethylene tank 8 by pipeline, described
5 lower interface of gas-liquid separator connects the left interface of the domethanizing column 7 by pipeline, and 7 lower interface of domethanizing column passes through pipeline
The left interface of the dethanizer 9 is connected, 13 lower interface of triple valve connects 4 upper right of the second heat exchanger by pipeline and connects
Mouthful, the 4 upper left interface of the second heat exchanger connects the 2 upper right interface of First Heat Exchanger, the First Heat Exchanger 2 by pipeline
Upper left interface connects the 14 bottom right interface of carbon dioxide ice maker by pipeline, and first precut 3 lower interface of tower passes through pipeline
The described second left interface of precut tower 10 is connected, the second precut column overhead outlet connects the dethanizer by pipeline
9 left interfaces, 9 tower bottom of dethanizer connect the carbon three by pipeline with the described second precut 10 tower bottom of tower and more recombinate
Divide outlet 11, interface passes through pipeline connection 6 lower interface of acetylene hydrogenation device in the ethane tower 9.
Wherein, the demethanation process of the domethanizing column 7 uses low-pressure process, and low-pressure process Recovery rate of ethylene is relatively high, is applicable in
Wider range；Catalyst is equipped in the acetylene hydrogenation device 6, the catalyst is palladium-silver；The First Heat Exchanger 2 and institute
Stating the second heat exchanger 4 is plate-fin heat exchanger, plate-fin heat exchanger good effect of heat exchange, and occupied area is small.
A kind of working method of device being prepared dry ice and separation ethylene using LNG cold energy of the invention, is specifically included:
(a) LNG divides through the LNG pump 12 and the triple valve 13 for two-way, sequentially enters second heat exchanger 4 all the way
Enter institute after converging with the First Heat Exchanger 2 vaporization released cold quantity, another way and from the LNG of the First Heat Exchanger 2 out
State carbon dioxide ice maker 14, the regulating valve 18 according to the cooling capacity control of LNG enter the carbon dioxide of the carbon dioxide ice maker 14 into
Tolerance, gas phase carbon dioxide absorb LNG cooling capacity in the carbon dioxide ice maker 14 and produce dry ice, and finished product dry ice passes through the dry ice
The dry ice outlet of manufacturing machine 14, which enters in the dry ice incubator 19, to be stored, and the LNG after vaporization heating is passed through the gas turbine
15 generate electricity for the generator 16；
(b) cracking gas enters the described first precut tower 3 after the First Heat Exchanger 2 pre-cooling and is separated, one He of carbon
More light component and two component of a small amount of carbon are in a gaseous form from the described first precut 3 tower top of tower outflow, into second heat exchange
Cryogenic separation in device 4, carbon one of the boiling point lower than -162 DEG C and two component of carbon are liquefied, hydrogen that boiling point is -252 DEG C and a small amount of lazy
Property gas be still gaseous state, the subsequent gas-liquid mixture enters the gas-liquid separator 5 and carries out gas-liquid separation, and hydrogen-rich gas is passed through institute
Stating acetylene hydrogenation device 6 is that the acetylene hydrogenation device 6 provides necessary hydrogen preparing ethylene, the carbon one being liquefied and two groups of carbon
To divide and the domethanizing column 7 is entered by the lower outlet of the gas-liquid separator 5, one component of carbon is flowed out by 7 tower top of domethanizing column,
Carbon two and more heavy constituent enter the dethanizer 9 by tower bottom, a large amount of carbon two and more recombinate that the first precut tower 3 separates
Divide and the described second precut tower 10 is entered by the tower bottom of the described first precut tower 3, is isolated through the described second precut tower 10
Carbon two and more light component and three component of a small amount of carbon the dethanizer 9, institute entered by the tower top of the described second precut tower 10
It states two component of carbon that dethanizer 9 is isolated and the acetylene hydrogenation device 6 is entered by tower top, two component of carbon and hydrogen-rich gas are being urged
Ethylene is generated under the action of agent, is stored to the ethylene tank 8, carbon three and more heavy constituent are by the dethanizer 9 and described
The tower bottom of two precut towers 10 flows out, and finally by the carbon three and more, heavy constituent outlet 11 is discharged.
The above are of the invention to illustrate, only highly preferred embodiment of the present invention, is not intended to limit the invention, it is all
Modification, equivalent replacement etc. within spirit and principle of the invention, are answered within the scope of the present invention.
Claims (7)
1. a kind of prepare dry ice using LNG cold energy and separate the device of ethylene, which is characterized in that including dry ice manufacture system and second
Alkene refining system, wherein the dry ice manufacture system includes: LNG pump (12), triple valve (13), carbon dioxide ice maker (14), combustion gas
Turbine (15), generator (16), high-pressure carbon dioxide air accumulator (17), dry ice incubator (19), the LNG pump (12) pass through pipe
Road connects the right interface of the triple valve (13), and the left interface of the triple valve (13) connects the carbon dioxide ice maker (14) by pipeline
Bottom right interface, high-pressure carbon dioxide air accumulator (17) outlet connect the carbon dioxide ice maker (14) entrance, institute by pipeline
It states carbon dioxide ice maker (14) outlet and the dry ice incubator (19), carbon dioxide ice maker (14) the upper right interface is connected by pipeline
It is connected the gas turbine (15) by pipeline, the gas turbine (15) is connected by axis with the generator (16)；It is described
Ethylene refining system includes: cracking gas tank (1), First Heat Exchanger (2), the first precut tower (3), the second heat exchanger (4), gas-liquid
Separator (5), acetylene hydrogenation device (6), domethanizing column (7), ethylene tank (8), dethanizer (9), carbon three and more heavy constituent row
It exports (11), the cracking gas tank (1) connects the First Heat Exchanger (2) lower-left interface, the First Heat Exchanger by pipeline
(2) bottom right interface connects the described first left interface of precut tower (3) by pipeline, and interface is logical on the first precut tower (3)
Piping connects the second heat exchanger (4) lower-left interface, and the second heat exchanger (4) bottom right interface passes through described in pipeline connection
Gas-liquid separator (5) left interface, interface is connected on the acetylene hydrogenation device (6) by pipeline on the gas-liquid separator (5)
Interface, the right interface of the acetylene hydrogenation device (6) connect the ethylene tank (8) by pipeline, connect under the gas-liquid separator (5)
Mouth connects the domethanizing column (7) left interface by pipeline, and domethanizing column (7) lower interface connects the de- second by pipeline
Alkane tower (9) left interface, triple valve (13) lower interface connects the second heat exchanger (4) upper right interface by pipeline, described
Second heat exchanger (4) upper left interface connects the First Heat Exchanger (2) upper right interface, the First Heat Exchanger (2) by pipeline
Upper left interface connects the carbon dioxide ice maker (14) bottom right interface by pipeline, and first precut tower (3) lower interface passes through
Pipeline connects the left interface of the dethanizer (9), and dethanizer (9) lower interface connects the carbon three and heavier by pipeline
Component outlet (11), interface passes through pipeline and connects acetylene hydrogenation device (6) lower interface on the ethane tower (9).
2. a kind of according to right 1 prepare dry ice using LNG cold energy and separate the device of ethylene, it is characterised in that: described
The demethanation process of domethanizing column (7) uses high-pressure process or low-pressure process.
3. a kind of according to right 1 prepare dry ice using LNG cold energy and separate the device of ethylene, it is characterised in that: described
Regulating valve (18) are equipped between high-pressure carbon dioxide air accumulator (17) and the carbon dioxide ice maker (14).
4. a kind of according to right 1 prepare dry ice using LNG cold energy and separate the device of ethylene, it is characterised in that: described
Catalyst is equipped in acetylene hydrogenation device (6), the catalyst is palladium or palladium-silver.
5. a kind of according to right 1 prepare dry ice using LNG cold energy and separate the device of ethylene, it is characterised in that: described
The second precut tower (10) that is connected, second pre-cut are additionally provided between first precut tower (3) and the dethanizer (9)
It cuts tower (10) and the carbon three and more heavy constituent outlet (11) is connected by pipeline.
6. a kind of according to right 1 prepare dry ice using LNG cold energy and separate the device of ethylene, it is characterised in that: described
First Heat Exchanger (2) and second heat exchanger (4) are pipe heat exchanger or plate-fin heat exchanger.
7. a kind of based on a kind of described in any item works for the device for preparing dry ice using LNG cold energy and separating ethylene of right 1~6
Make method, it is characterised in that: specifically include:
(a) LNG is divided into two-way through the LNG pump (12) and the triple valve (13), sequentially enters second heat exchanger all the way
(4) and the First Heat Exchanger (2) vaporize released cold quantity, another way with from the First Heat Exchanger (2) come out LNG converge after
Into the carbon dioxide ice maker (14), the regulating valve (18) enters the carbon dioxide ice maker (14) according to the cooling capacity control of LNG
Carbon dioxide amount, gas phase carbon dioxide absorbs LNG cooling capacity in the carbon dioxide ice maker (14) and produces dry ice, and finished product is dry
Ice enters storage in the dry ice incubator (19) by the dry ice outlet of the carbon dioxide ice maker (14), after vaporization heating
LNG is passed through the gas turbine (15) and generates electricity for the generator (16)；
(b) cracking gas enters the described first precut tower (3) after the First Heat Exchanger (2) pre-cooling and is separated, one He of carbon
More light component and two component of a small amount of carbon are changed in a gaseous form from the described first precut tower (3) tower top outflow into described second
Cryogenic separation in hot device (4), carbon one of the boiling point lower than -162 DEG C and two component of carbon are liquefied, the hydrogen and lack that boiling point is -252 DEG C
Measuring inert gas is still gaseous state, and the subsequent gas-liquid mixture enters the gas-liquid separator (5) and carries out gas-liquid separation, hydrogen-rich gas
Being passed through the acetylene hydrogenation device (6) is that the acetylene hydrogenation device (6) provides necessary hydrogen preparing ethylene, the carbon being liquefied
One and two component of carbon by the gas-liquid separator (5) lower outlet enter the domethanizing column (7), one component of carbon is by the piptonychia
The outflow of alkane tower (7) tower top, carbon two and more heavy constituent enter the dethanizer (9) by tower bottom, the first precut tower (3) point
From a large amount of carbon two and more heavy constituent by the described first precut tower (3) tower bottom enter the described second precut tower (10), warp
The carbon two and more light component and three component of a small amount of carbon that the second precut tower (10) is isolated are by the described second precut tower
(10) tower top enters the dethanizer (9), and two component of carbon that the dethanizer (9) is isolated enters the second by tower top
Alkynes hydrogenation plant (6), two component of carbon and hydrogen-rich gas generate ethylene under the effect of the catalyst, store to the ethylene tank (8),
Carbon three and more heavy constituent are flowed out by the tower bottom of the dethanizer (9) and the second precut tower (10), finally by the carbon
Three and more heavy constituent outlet (11) discharge.
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| CN201910444287.XA CN110330018B (en) | 2019-05-27 | 2019-05-27 | Device for preparing dry ice and separating ethylene by using LNG cold energy and working method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114087846A (en) * | 2022-01-17 | 2022-02-25 | 杭州制氧机集团股份有限公司 | Device for producing dry ice by coupling photoelectric hydrogen production energy storage and cold energy recovery and use method |
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