CN107021876A - CCUS systems and process applied to petroleum and petrochemical industry - Google Patents
CCUS systems and process applied to petroleum and petrochemical industry Download PDFInfo
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- CN107021876A CN107021876A CN201710371919.5A CN201710371919A CN107021876A CN 107021876 A CN107021876 A CN 107021876A CN 201710371919 A CN201710371919 A CN 201710371919A CN 107021876 A CN107021876 A CN 107021876A
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- 239000003208 petroleum Substances 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 16
- 230000008569 process Effects 0.000 title claims abstract description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 196
- 239000007789 gas Substances 0.000 claims abstract description 76
- 238000010521 absorption reaction Methods 0.000 claims abstract description 42
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 37
- 238000002407 reforming Methods 0.000 claims abstract description 33
- 229910001868 water Inorganic materials 0.000 claims abstract description 32
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 26
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 25
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000006073 displacement reaction Methods 0.000 claims abstract description 24
- 239000001301 oxygen Substances 0.000 claims abstract description 24
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 24
- 238000002347 injection Methods 0.000 claims abstract description 19
- 239000007924 injection Substances 0.000 claims abstract description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000002485 combustion reaction Methods 0.000 claims abstract description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical group [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000003546 flue gas Substances 0.000 claims abstract description 12
- 239000003345 natural gas Substances 0.000 claims abstract description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 9
- 238000009833 condensation Methods 0.000 claims abstract 2
- 230000005494 condensation Effects 0.000 claims abstract 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 99
- 230000008676 import Effects 0.000 claims description 34
- 239000007788 liquid Substances 0.000 claims description 33
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 239000000047 product Substances 0.000 claims description 25
- 239000007795 chemical reaction product Substances 0.000 claims description 15
- 230000018044 dehydration Effects 0.000 claims description 14
- 238000006297 dehydration reaction Methods 0.000 claims description 14
- 239000012071 phase Substances 0.000 claims description 12
- 239000012263 liquid product Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 6
- 239000002250 absorbent Substances 0.000 claims description 5
- 230000002745 absorbent Effects 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 3
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000013589 supplement Substances 0.000 claims description 3
- 230000009466 transformation Effects 0.000 claims description 3
- 238000010795 Steam Flooding Methods 0.000 claims description 2
- 239000002002 slurry Substances 0.000 claims description 2
- 239000003463 adsorbent Substances 0.000 claims 1
- 239000000567 combustion gas Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 12
- 239000000446 fuel Substances 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 4
- 238000001308 synthesis method Methods 0.000 abstract description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 31
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 22
- 239000001569 carbon dioxide Substances 0.000 description 7
- 241000196324 Embryophyta Species 0.000 description 6
- 230000008901 benefit Effects 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 2
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000006057 reforming reaction Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 241000208340 Araliaceae Species 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 235000005035 Panax pseudoginseng ssp. pseudoginseng Nutrition 0.000 description 1
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000002079 cooperative effect Effects 0.000 description 1
- 230000000875 corresponding effect Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 235000008434 ginseng Nutrition 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000003129 oil well Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000010010 raising Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 230000037351 starvation Effects 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
- C07C41/40—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation
- C07C41/42—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation by distillation
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B33/00—Steam-generation plants, e.g. comprising steam boilers of different types in mutual association
- F22B33/18—Combinations of steam boilers with other apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
- F23L7/007—Supplying oxygen or oxygen-enriched air
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/32—Direct CO2 mitigation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/70—Combining sequestration of CO2 and exploitation of hydrocarbons by injecting CO2 or carbonated water in oil wells
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Mining & Mineral Resources (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Mechanical Engineering (AREA)
- Geology (AREA)
- Physics & Mathematics (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Thermal Sciences (AREA)
- Fluid Mechanics (AREA)
- Environmental & Geological Engineering (AREA)
- Combustion & Propulsion (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of CCUS systems and process applied to petroleum and petrochemical industry, the CCUS systems are by the isolated nitrogen of air and oxygen-enriched, oxygen-enriched introducing gas-steam boiler and fuel natural gas mixed combustion, an obtained flue gas part is mixed into boiler as circulating air with oxygen-enriched, another part carries out tri-reforming with fuel natural gas in tri-reforming device, and reacting obtained synthesis gas has two kinds of Land use systems：One kind is that direct re-injection oil reservoir carries out the displacement of reservoir oil, and another is to enter paste state bed reactor one-step synthesis method DME, and condensed device condensation obtains CO step by step by separator, absorption plant, rectifier unit2, DME, methanol and water, the N that air-separating plant is obtained2, gas-steam boiler produce steam, CO2The CO that separator is isolated2Oil reservoir oil displacement is injected simultaneously.Present invention joint oxygen-enriched combustion technology, natural gas and the triple adjusting techniques of flue gas and one-step synthesis method DME technology, obtain multiple gases and DME, methanol, water carry out recycling.
Description
Technical field
The present invention relates to the technical field of the oil field utilization of resources, and in particular to a kind of CCUS applied to petroleum and petrochemical industry
System and process.
Background technology
Global warming causes earth's surface mean temperature to rise, extreme climate occurs and seawater the problems such as be acidified into
The significant problem attracted attention for the world today, has badly influenced the survival and development of the mankind.Cause the root of global warming
It is greenhouse gases CO2Discharge, therefore reduce CO2Discharge is most important for alleviating climate warming.
In recent years, CCS (Carbon Capture and Storage) is always the focus of international concern, and China
As developing country, while being evolving economical, the dynamics of emission reduction also is being increased, and is combining the reality of this country, in CCS
On the basis of propose CCUS (Carbon Capture, Utilization and Storage), the i.e. trapping of carbon dioxide,
Using with sealing up for safekeeping.CCUS technologies for control CO2 emission, realize sustainable development as an emerging cutting edge technology
Play vital effect.China faces the high carbonization problem of serious energy resource structure, and situation allows of no optimist, and petroleum and petrochemical industry
The share of carbon emission shared by industry is quite big, and the pressure and constraint for tackling climate change increasingly increase.But from the sector
Development characteristic is set out, and it is within sight that alleviation problem, which further deteriorates,.
CCUS technologies are related to the trapping of carbon dioxide, transport and seal up for safekeeping and multiple sport technique segments such as utilize, to whole production
Its cost height is the key factor for restricting its development for industry chain.For petroleum and petrochemical industry, in order to meet oil
The demand of exploitation, improves oil recovery, generally injects carbon dioxide into oil reservoir and carries out the displacement of reservoir oil, most of source of the gas carrys out spontaneous combustion coal
CO in the flue gas of power plant2, and the main component in flue gas is nitrogen, the content of carbon dioxide is relatively low, so as to lead
Cause separating energy consumption big, trapping cost is high；The CO trapped2Again by pipeline transportation to corresponding oil well at, virtually again increase
The cost of higher pipe laying.Therefore, the resource in whole technique how is rationally utilized, obtained product is subjected to resource
Change and utilize, so as to construct a higher Energy Polygeneration System of flexibility, it will being one fundamentally improves economy
Shortcut.
The content of the invention
It is an object of the invention to overcome the shortcomings of above-mentioned background technology, and provide a kind of applied to petroleum and petrochemical industry
CCUS systems, fully around the flue gas produced by gas-steam boiler in oil field, joint oxygen-enriched combustion technology, natural gas and cigarette
The triple adjusting techniques of gas and one-step synthesis method DME (dimethyl ether) technology, obtained multiple gases and fuel-grade DME, methanol, water
Recycling is carried out, a kind of process of the system is additionally provided.
To achieve the above object, the designed CCUS systems for being applied to petroleum and petrochemical industry of the present invention, including air separation
Device, gas-steam boiler, tri-reforming device, heat exchanger, paste state bed reactor, condenser, gas-liquid separator, absorption tower,
Pressure-swing absorption apparatus, Dehydration of methanol device, DME rectifying columns, CO2Separator, methanol rectifying tower；
The air-separating plant, which is provided with, is used for the nitrogen outlet that re-injection oil reservoir carries out the displacement of reservoir oil, the air-separating plant
Oxygen-enriched outlet is connected by the oxygen-enriched import of the first pipeline and gas-steam boiler, and the first flue gas of the gas-steam boiler goes out
Mouth is connected with the first pipeline, and the second exhanst gas outlet of the gas-steam boiler is connected with the gas approach of tri-reforming device,
The gas-steam boiler also sets up Imported gas and the steam (vapor) outlet of the displacement of reservoir oil, the combustion and steam is carried out for re-injection oil reservoir
The steam (vapor) outlet of boiler is connected by branch road with the steam inlet of tri-reforming device, the gas outlet of the gas-steam boiler
It is connected with the fuel gas inlet of tri-reforming device；
The syngas outlet of the tri-reforming device is connected by the synthesis gas import of the second pipeline and heat exchanger, described
Heat exchanger high-temperature synthesis gas outlet be connected with the high-temperature synthesis gas import of paste state bed reactor, the paste state bed reactor it is anti-
Answer the reaction product import of product exit and heat exchanger to connect, the low-temp reaction product exit of the heat exchanger and condenser it is low
Warm reaction product import connection, the gas-liquid mixture outlet and the gas-liquid mixture import of gas-liquid separator of the condenser connect
Connect, the gas phase import on the gaseous phase outlet of the gas-liquid separator and absorption tower is connected, the liquid-phase outlet of the gas-liquid separator with
The first import connection of DME rectifying columns；
The absorbing liquid outlet on the absorption tower is connected with the absorbing liquid import of Dehydration of methanol device, and the methanol dehydration is anti-
The product exit of device is answered to be connected with the second import of DME rectifying columns, the DME rectifying columns are additionally provided with DME outlets, the DME essences
The crude carbinol solution inlet port of the crude carbinol taphole and methanol rectifying tower that evaporate tower is connected, the methanol outlet of the methanol rectifying tower
It is connected with the methanol import on absorption tower, the water out of the methanol rectifying tower and the water inlet of gas-steam boiler are connected.
In above-mentioned technical proposal, it also includes pressure-swing absorption apparatus, and top gas outlet and the transformation on the absorption tower are inhaled
The gas feed connection of adsorption device, the gas vent of the pressure-swing absorption apparatus is connected with the second pipeline.
In above-mentioned technical proposal, it also includes CO2Separator, the mixed gas outlet and CO of the DME rectifying columns2Separation
The mixed gas import connection of device, the CO2Separator is additionally provided with the CO that the displacement of reservoir oil is carried out for re-injection oil reservoir2Outlet.
In above-mentioned technical proposal, the CO2Separator is the separator of diaphragm type.
In above-mentioned technical proposal, the pipeline between the water out of the methanol rectifying tower and the water inlet of gas-steam boiler
On be provided with pump.
In above-mentioned technical proposal, the absorbent on the absorption tower is methanol.
In above-mentioned technical proposal, the reaction temperature of the paste state bed reactor is 260-270 DEG C, and reaction pressure is 3-
5MPa。
In above-mentioned technical proposal, the tower top temperature of the DME rectifying columns is 20-90 DEG C, and column bottom temperature is 150-220 DEG C,
Pressure is 0.2-2.2MPa.
In above-mentioned technical proposal, the tower top temperature of the methanol rectifying tower is 40-90 DEG C, and column bottom temperature is 80-150 DEG C,
Pressure is 0.1-0.8MPa.
Present invention also offers a kind of process of the CCUS systems applied to petroleum and petrochemical industry, including following step
Suddenly：
1) air is rich by the isolated nitrogen of air-separating plant and oxygen-enriched, the direct re-injection oil reservoir progress displacement of reservoir oil of nitrogen
Oxygen introduces gas-steam boiler and obtains steam and flue gas with natural gas mixed combustion；Wherein, the part injection oil reservoir of steam drives
Oil, another part as tri-reforming supplement steam；A part for flue gas is followed with the oxygen-enriched gas-steam boiler that is mixed into
Ring is used, and another part enters tri-reforming device and carries out tri-reforming with natural gas, oxygen, steam, generates synthesis gas；
2) part directly re-injection oil reservoir carries out the displacement of reservoir oil in the synthesis gas obtained by tri-reforming device, and another part is by changing
After hot device is exchanged heat with the reacted reaction product of paste state bed reactor, reacted into paste state bed reactor, slurry bed system
Reactor interior reaction temperature is 260-270 DEG C, and reaction pressure is 3-5MPa；
4) reaction product of paste state bed reactor is condensed to 30-40 DEG C after heat exchanger exchanges heat into condenser, wherein,
Methanol steam and DME steam are condensed into liquid product, fixed gas CO, CO2、H2And the DME gases not being condensed are produced as gas phase
Thing, liquid product and gas-phase product are separated into gas-liquid separator, and gas-phase product enters in absorption tower and passes through methanol absorption
Afterwards, fixed gas CO, H2Discharged at the top of absorption tower, reclaimed by pressure-swing absorption apparatus and be recycled into the second pipe as synthesis material
Road；
5) absorb tower bottom absorbing liquid reacted into Dehydration of methanol device after obtain containing dimethyl ether, water and
CO2Product, the liquid product of product and gas-liquid separator together enters DME rectifying columns, enters under 0.2-2.2MPa pressure
Row rectifying is separated, and tower top temperature is 20-90 DEG C, and column bottom temperature is 150-220 DEG C, and rectifying goes out DME；
6) mixed gas that DME rectifying columns are obtained enters CO2Separator, the CO isolated2Inject oil reservoir oil displacement；DME rectifying
The crude carbinol solution that tower is obtained enters methanol rectifying tower, and rectifying separation is carried out under 0.1-0.8MPa pressure, methanol is isolated
And water, methanol return absorption tower, water is by being pumped into gas-steam boiler recycling.
Compared with prior art, the invention has the advantages that：
First, the present invention by oxygen-enriched combustion technology by introducing gas-steam boiler in oil field, in this process, due to
Without N in air2Participation, reduce NOx discharge so that pollutant emission has obtained Collaborative Control, protect big compression ring
Border；The participation of a large amount of oxygen not only causes fuel combustion more abundant simultaneously, improves the efficiency of combustion of boiler, also causes what is produced
CO2Concentration is higher, and the reactant (CO of abundance is provided for follow-up tri-reforming2、O2), so as to synthesize more fuel DME.
Fuel DME has good burning performance, and the thermal efficiency is high, without residual night, without black smoke in combustion process, is a kind of high-quality, the fuel of cleaning, will not
Ozone layer is caused harm, effectively environmental protection, and the resource profile of China is the few gas of oil starvation, so it is expected to turn into main
Oil replaces product.
Second, the N that the present invention can obtain air-separating plant2, gas-steam boiler produce steam, CO2Separation dress
Put the CO isolated2Oil reservoir oil displacement is injected simultaneously, is realized " note of a stove three ", the recovery ratio in oil field is improved, and realizes environment and economical
Double benefit, obtained methanol is as absorbent, and inner loop is utilized, and obtained water is as boiler feedwater, by being pumped into
Boiler produces steam, can be good at recycling, produces considerable economic benefit.
Third, the present invention realizes the raisings of DME conversion ratios and energy-saving in one-step synthesis method DME separating technology
Purpose, by setting heat exchanger, material synthesis gas are exchanged heat with reacted gaseous product, material synthesis gas is increased to ginseng
It is that subsequent technique reduces disappearing for cold energy while reducing reacted gaseous product temperature with the temperature (270 DEG C) of reaction
Consumption.Increased Dehydration of methanol device, reactant comes from absorbent methanol so that DME conversion ratio is greatly improved.
Fourth, resource can be obtained and utilized on the spot in the whole system of the present invention, pipe laying cost, long-distance transport are saved
Expense and fixed gas recovery cost, the fuel natural gas needed for gas-steam boiler can be obtained directly from oil field, and tri-reforming is anti-
Answer required raw material CH4、CO2、H2O、O2It can just be obtained in abundance, direct burner hearth, using O2/CO2Combustion technology, is saved high
CO2Trap the fixed gas at the top of cost, and absorption tower out and useful constituent H is reclaimed by pressure-variable adsorption2, CO make synthesis gas
Feedstock circulation.
Fifth, the present invention, which is applied to petroleum and petrochemical industry, has good prospect, carbon dioxide drive is special/super for improving
Recovery of A Medium-low Permeability Oil Reservoir has positive effect, through geologic assessment, and the petroleum-in-place that China there are about 10,000,000,000 tons is adapted to use
Carbon dioxide drive.By all implementation carbon dioxide drive measuring and calculating, it is contemplated that 700,000,000 tons to 1,400,000,000 tons of recoverable reserves can be increased.Separately
Outside, the product DME of production can substitute liquefied petroleum gas, the not enough situation of respite oil supply.
Brief description of the drawings
Fig. 1 is a kind of structural representation of CCUS systems applied to petroleum and petrochemical industry；
Embodiment
Describe the performance of the present invention in detail with reference to case study on implementation, but they do not constitute the limit to the present invention
It is fixed, it is only for example.Simultaneously by illustrating that advantages of the present invention will become clearer and be readily appreciated that.
A kind of CCUS systems applied to petroleum and petrochemical industry of the invention, including air-separating plant 1, combustion as shown in the figure
Gas steam boiler 2, tri-reforming device 3, heat exchanger 4, paste state bed reactor 5, condenser 6, gas-liquid separator 7, absorption tower 8,
Dehydration of methanol device 10, DME rectifying columns 11, methanol rectifying tower 13；
The air-separating plant 1, which is provided with, is used for the nitrogen outlet 1.1 that re-injection oil reservoir carries out the displacement of reservoir oil, the air separation dress
The oxygen-enriched outlet 1.2 for putting 1 is connected by the first pipeline 15.1 with the oxygen-enriched import 2.1 of gas-steam boiler 2, the combustion and steam
First exhanst gas outlet 2.2 of boiler 2 is connected with the first pipeline 15.1, the second exhanst gas outlet 2.3 of the gas-steam boiler 2 with
The gas approach 3.1 of tri-reforming device 3 is connected, and the gas-steam boiler 2 also sets up Imported gas 2.4 and for re-injection
Oil reservoir carries out the steam (vapor) outlet 2.5 of the displacement of reservoir oil, and the steam (vapor) outlet 2.5 of the gas-steam boiler 2 passes through branch road and tri-reforming
The steam inlet 3.2 of device 3 is connected, the gas outlet 2.6 of the gas-steam boiler 2 and the fuel gas inlet of tri-reforming device 3
3.3 connection；
The synthesis gas import that the syngas outlet 3.4 of the tri-reforming device 3 passes through the second pipeline 15.2 and heat exchanger 4
4.1 connections, the high-temperature synthesis gas outlet 4.2 of the heat exchanger 4 is connected with the high-temperature synthesis gas import 5.1 of paste state bed reactor 5,
The reacting product outlet 5.2 of the paste state bed reactor 5 is connected with the reaction product import 4.3 of heat exchanger 4, the heat exchanger 4
Low-temp reaction product exit 4.4 be connected with the low-temp reaction product inlet 6.1 of condenser 6, the gas-liquid mixed of the condenser 6
Thing outlet 6.2 is connected with the gas-liquid mixture import 7.1 of gas-liquid separator 7, the gaseous phase outlet 7.2 of the gas-liquid separator 7 and
The gas phase import 8.1 on absorption tower 8 is connected, the liquid-phase outlet 7.3 of the gas-liquid separator 7 and the first import of DME rectifying columns 11
11.1 connections；
The absorbent on the absorption tower 8 is methanol, absorbing liquid outlet 8.2 and the Dehydration of methanol device on the absorption tower 8
10 absorbing liquid import 10.1 is connected, the product exit 10.2 of the Dehydration of methanol device 10 and the second of DME rectifying columns 11
Import 11.2 is connected, and the DME rectifying columns 11 are additionally provided with DME outlets 11.3, the crude carbinol taphole of the DME rectifying columns 11
11.4 are connected with the crude carbinol solution inlet port 13.1 of methanol rectifying tower 13, and the methanol outlet 13.2 of the methanol rectifying tower 13 is with inhaling
The methanol import 8.4 for receiving tower 8 is connected, the water out 13.3 of the methanol rectifying tower 13 and the water inlet 2.7 of gas-steam boiler 2
It is provided with connection, the pipeline between the water out 13.3 of the methanol rectifying tower 13 and the water inlet 2.7 of gas-steam boiler 2
Pump 14.The top gas outlet 8.3 on the absorption tower 8 is connected with the gas feed 9.1 of pressure-swing absorption apparatus 9, and the transformation is inhaled
The gas vent 9.2 of adsorption device 9 is connected with the second pipeline 15.2.The mixed gas outlet 11.5 and CO of the DME rectifying columns 112
The mixed gas import 12.1 of separator 12 is connected, the CO2Separator 12 is additionally provided with the CO that the displacement of reservoir oil is carried out for re-injection oil reservoir2
Outlet 12.2.The CO2Separator 12 is the separator of diaphragm type.
Process of the present invention applied to the CCUS systems of petroleum and petrochemical industry, comprises the following steps：
1) air is rich by the isolated nitrogen of air-separating plant 1 and oxygen-enriched, the direct re-injection oil reservoir progress displacement of reservoir oil of nitrogen
Oxygen introduces gas-steam boiler 2 and obtains steam and flue gas (containing the CO that mass percent is 65% with natural gas mixed combustion2、
Mass percent is 30% H2O)；Wherein, the part injection oil reservoir oil displacement of steam, another part is used as tri-reforming
Supplement steam；A part for flue gas is recycled with the oxygen-enriched gas-steam boiler 2 that is mixed into, and it is anti-that another part enters tri-reforming
Device 3 is answered to carry out tri-reforming, generation synthesis gas (H with natural gas, oxygen, steam2、CO、H2O)；Wherein, tri-reforming master
Reacting has four：The CO 2 reforming reaction of methane, the steam reforming reaction of methane, the partial oxidation reaction of methane and
The complete oxidation of methane, the first two reaction is strong endothermic reaction, and latter two reaction is strong exothermal reaction, when this four reactions
When carrying out simultaneously, the high shortcoming of endothermic reforming reaction is just overcome, reaction is in " neutral " state, greatly reduces energy
It is lost, reaction equation is：
CH4+CO2=2CO+2H2(ΔH0=247.3kJ/mol)
CH4+H2O=CO+3H2(ΔH0=206.3kJ/mol)
CH4+1/2O2=CO+2H2(ΔH0=-35.6kJ/mol)
CH4+2O2=CO2+2H2O(ΔH0=-880kJ/mol)
Tri-reforming device is placed at gas-steam boiler furnace outlet, makes full use of 1000 DEG C of furnace outlet hot conditions
Left and right and on the spot raw material (natural gas, oxygen, flue gas).
2) part directly re-injection oil reservoir carries out the displacement of reservoir oil in the synthesis gas of the gained of tri-reforming device 3, and another part passes through
After heat exchanger 4 is exchanged heat with the reacted reaction product of paste state bed reactor 5, one-step method is carried out into paste state bed reactor 5
DME reactions are synthesized, the interior reaction temperature of paste state bed reactor 5 is 260-270 DEG C, and reaction pressure is 3-5MPa；Wherein, one-step method is closed
Refer to synthesis gas in paste state bed reactor into DME while completing methanol-fueled CLC and Dehydration of methanol.The first synthesized in reaction
Alcohol can be dehydrated generation DME quickly, and the H2O taken off is consumed by CO again, has broken the Equilibrium limit of methanol synthesis reaction.By
In the synergy of these reactions, strong cooperative effect is generated, the conversion ratio of synthesis gas is considerably increased.Reaction equation is：
CO+2H2→CH3OH+90.4kJ
2CH3OH→CH3OCH3+H20+23.4kJ
CO+H2O→H2+CO2+40.9kJ
3) reaction product of paste state bed reactor 5 is condensed to 30-40 DEG C after the heat exchange of heat exchanger 4 into condenser 6, its
In, methanol steam and DME steam are condensed into liquid product, fixed gas CO, CO2、H2And the DME gases not being condensed are as gas phase
Product, liquid product and gas-phase product are separated into gas-liquid separator 7, and gas-phase product enters in absorption tower 8 and passes through methanol
After absorption, fixed gas CO, H2Discharged by the top of absorption tower 8, reclaimed by pressure-swing absorption apparatus 9 and be recycled into the as synthesis material
Two pipelines 15.2；
4) absorbing liquid of the bottom of absorption tower 8 is obtained containing dimethyl ether, water after being reacted into Dehydration of methanol device 10
And CO2Product, product and the liquid product of gas-liquid separator 7 together enter DME rectifying columns 11, under 0.2-2.2MPa pressure
Rectifying separation is carried out, tower top temperature is 20-90 DEG C, and column bottom temperature is 150-220 DEG C, and rectifying goes out DME；
5) mixed gas that DME rectifying columns 11 are obtained enters CO2Separator 12, the CO isolated2Inject oil reservoir oil displacement；DME
The crude carbinol solution that rectifying column 11 is obtained enters methanol rectifying tower 13, and rectifying separation is carried out under 0.1-0.8MPa pressure, point
First alcohol and water is separated out, methanol returns to absorption tower 8, and water is sent into gas-steam boiler 2 by pump 14 and recycled.The steaming that boiler is produced
The N that vapour is obtained with space division2、CO2The CO that separator is isolated2Oil reservoir oil displacement is injected simultaneously, is realized " note of a stove three ".
More than, it is only the embodiment of the present invention, it is noted that any those skilled in the art are in this hair
In bright disclosed technical scope, the change or replacement that can be readily occurred in should be all included within the scope of the present invention.
Claims (10)
1. a kind of CCUS systems applied to petroleum and petrochemical industry, it is characterised in that：Steamed including air-separating plant (1), combustion gas
Boiler furnace (2), tri-reforming device (3), heat exchanger (4), paste state bed reactor (5), condenser (6), gas-liquid separator (7),
Absorption tower (8), Dehydration of methanol device (10), DME rectifying columns (11), methanol rectifying tower (13)；
The air-separating plant (1), which is provided with, is used for the nitrogen outlet (1.1) that re-injection oil reservoir carries out the displacement of reservoir oil, the air separation dress
The oxygen-enriched outlet (1.2) for putting (1) is connected by the first pipeline (15.1) with the oxygen-enriched import (2.1) of gas-steam boiler (2), institute
The first exhanst gas outlet (2.2) for stating gas-steam boiler (2) is connected with the first pipeline (15.1), the gas-steam boiler (2)
The second exhanst gas outlet (2.3) be connected with the gas approach (3.1) of tri-reforming device (3), the gas-steam boiler (2) also
Imported gas (2.4) is set and the steam (vapor) outlet (2.5) of the displacement of reservoir oil, the gas-steam boiler (2) are carried out for re-injection oil reservoir
Steam (vapor) outlet (2.5) be connected by branch road with the steam inlet (3.2) of tri-reforming device (3), the gas-steam boiler
(2) gas outlet (2.6) is connected with the fuel gas inlet (3.3) of tri-reforming device (3)；
The syngas outlet (3.4) of the tri-reforming device (3) passes through the second pipeline (15.2) and the synthesis gas of heat exchanger (4)
Import (4.1) is connected, the high-temperature synthesis gas outlet (4.2) of the heat exchanger (4) and the high-temperature synthesis gas of paste state bed reactor (5)
Import (5.1) is connected, the reacting product outlet (5.2) of the paste state bed reactor (5) and the reaction product import of heat exchanger (4)
(4.3) connect, the low-temp reaction product exit (4.4) of the heat exchanger (4) and the low-temp reaction product inlet of condenser (6)
(6.1) connect, the gas-liquid mixture outlet (6.2) and the gas-liquid mixture import of gas-liquid separator (7) of the condenser (6)
(7.1) connect, the gaseous phase outlet (7.2) of the gas-liquid separator (7) is connected with the gas phase import (8.1) of absorption tower (8), described
The liquid-phase outlet (7.3) of gas-liquid separator (7) is connected with the first import (11.1) of DME rectifying columns (11)；
The absorbing liquid outlet (8.2) of the absorption tower (8) is connected with the absorbing liquid import (10.1) of Dehydration of methanol device (10),
The product exit (10.2) of the Dehydration of methanol device (10) is connected with the second import (11.2) of DME rectifying columns (11), institute
State DME rectifying columns (11) be additionally provided with DME outlet (11.3), the crude carbinol taphole (11.4) of the DME rectifying columns (11) with
Methanol rectifying tower (13) crude carbinol solution inlet port (13.1) connection, the methanol outlet (13.2) of the methanol rectifying tower (13) with
Methanol import (8.4) connection on absorption tower (8), the water out (13.3) and gas-steam boiler of the methanol rectifying tower (13)
(2) water inlet (2.7) connection.
2. the CCUS systems according to claim 1 applied to petroleum and petrochemical industry, it is characterised in that：It also includes transformation
Adsorbent equipment (9), the top gas outlet (8.3) and the gas feed (9.1) of pressure-swing absorption apparatus (9) of the absorption tower (8)
Connection, the gas vent (9.2) of the pressure-swing absorption apparatus (9) is connected with the second pipeline (15.2).
3. the CCUS systems according to claim 2 applied to petroleum and petrochemical industry, it is characterised in that：It also includes CO2Point
From device (12), the mixed gas outlet (11.5) and CO of the DME rectifying columns (11)2The mixed gas import of separator (12)
(12.1) connect, the CO2Separator (12) is additionally provided with the CO that the displacement of reservoir oil is carried out for re-injection oil reservoir2Export (12.2).
4. the CCUS systems according to claim 3 applied to petroleum and petrochemical industry, it is characterised in that：The CO2Separator
(12) it is the separator of diaphragm type.
5. the CCUS systems according to claim 4 applied to petroleum and petrochemical industry, it is characterised in that：The methanol rectification
Pump (14) is provided with pipeline between the water out (13.3) of tower (13) and the water inlet (2.7) of gas-steam boiler (2).
6. the CCUS systems applied to petroleum and petrochemical industry according to claim 1 or 2 or 3 or 4 or 5, it is characterised in that：
The absorbent of the absorption tower (8) is methanol.
7. the CCUS systems according to claim 6 applied to petroleum and petrochemical industry, it is characterised in that：The slurry bed system is anti-
The reaction temperature for answering device (5) is 260-270 DEG C, and reaction pressure is 3-5MPa.
8. the CCUS systems according to claim 7 applied to petroleum and petrochemical industry, it is characterised in that：The DME rectifying
The tower top temperature of tower (11) is 20-90 DEG C, and column bottom temperature is 150-220 DEG C, and pressure is 0.2-2.2MPa.
9. the CCUS systems according to claim 8 applied to petroleum and petrochemical industry, it is characterised in that：The methanol rectification
The tower top temperature of tower (13) is 40-90 DEG C, and column bottom temperature is 80-150 DEG C, and pressure is 0.1-0.8MPa.
10. the process of the CCUS systems of petroleum and petrochemical industry is applied to described in a kind of utilization claim 1-9 any one,
It is characterised in that it includes following steps：
1) air is oxygen-enriched by air-separating plant (1) isolated nitrogen and oxygen-enriched, the direct re-injection oil reservoir progress displacement of reservoir oil of nitrogen
Introduce gas-steam boiler (2) and obtain steam and flue gas with natural gas mixed combustion；Wherein, the part injection oil reservoir of steam drives
Oil, another part as tri-reforming supplement steam；A part for flue gas is mixed into gas-steam boiler (2) with oxygen-enriched
Recycle, another part enters tri-reforming device (3) and carries out tri-reforming, generation synthesis with natural gas, oxygen, steam
Gas；
2) part directly re-injection oil reservoir carries out the displacement of reservoir oil in the synthesis gas obtained by tri-reforming device (3), and another part is by changing
After hot device (4) is exchanged heat with paste state bed reactor (5) reacted reaction product, one is carried out into paste state bed reactor (5)
Footwork synthesis DME reactions, paste state bed reactor (5) interior reaction temperature is 260-270 DEG C, and reaction pressure is 3-5MPa；
3) reaction product of paste state bed reactor (5) enters condenser (6) condensation to 30-40 DEG C after heat exchanger (4) heat exchange,
Wherein, methanol steam and DME steam are condensed into liquid product, fixed gas CO, CO2、H2And the DME gases not being condensed are as gas
Phase product, liquid product and gas-phase product are separated into gas-liquid separator (7), and gas-phase product, which enters in absorption tower (8), to pass through
Cross after methanol absorption, fixed gas CO, H2Discharged at the top of absorption tower (8), reclaimed by pressure-swing absorption apparatus (9) and make synthesis material
It is recycled into the second pipeline (15.2)；
4) absorbing liquid of absorption tower (8) bottom is obtained containing dimethyl ether, water after being reacted into Dehydration of methanol device (10)
And CO2Product, the liquid product of product and gas-liquid separator (7) together enters DME rectifying columns (11), 0.2-2.2MPa's
Rectifying separation is carried out under pressure, tower top temperature is 20-90 DEG C, and column bottom temperature is 150-220 DEG C, and rectifying goes out DME；
5) mixed gas that DME rectifying columns (11) are obtained enters CO2Separator (12), the CO isolated2Inject oil reservoir oil displacement；DME
The crude carbinol solution that rectifying column (11) is obtained enters methanol rectifying tower (13), and rectifying point is carried out under 0.1-0.8MPa pressure
From isolating first alcohol and water, methanol returns to absorption tower (8), water is sent into gas-steam boiler (2) by pump (14) and recycled.
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| CN114482927A (en) * | 2021-12-31 | 2022-05-13 | 西安本清化学技术有限公司 | Green low-carbon development system and method for thickened oil |
| CN114482927B (en) * | 2021-12-31 | 2024-06-07 | 西安本清化学技术有限公司 | Green low-carbon development system and method for thickened oil |
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| CN102431974A (en) * | 2011-09-23 | 2012-05-02 | 山东大学 | Oxygen-enriched combustion poly-generation process and equipment for steam injection boiler in oil field |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107575190A (en) * | 2017-09-25 | 2018-01-12 | 中国石油大学(华东) | One kind is based on optimal flue gas CO2The CCUS systems and its method of work of accumulation rate production of heavy oil reservoir |
| CN107575190B (en) * | 2017-09-25 | 2018-08-24 | 中国石油大学(华东) | One kind being based on optimal flue gas CO2The CCUS systems and its working method of accumulation rate production of heavy oil reservoir |
| CN114482927A (en) * | 2021-12-31 | 2022-05-13 | 西安本清化学技术有限公司 | Green low-carbon development system and method for thickened oil |
| CN114482927B (en) * | 2021-12-31 | 2024-06-07 | 西安本清化学技术有限公司 | Green low-carbon development system and method for thickened oil |
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