CN100510021C - Flow for separating outflow from hydrogenation reaction - Google Patents
Flow for separating outflow from hydrogenation reaction Download PDFInfo
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- CN100510021C CN100510021C CNB2007100010499A CN200710001049A CN100510021C CN 100510021 C CN100510021 C CN 100510021C CN B2007100010499 A CNB2007100010499 A CN B2007100010499A CN 200710001049 A CN200710001049 A CN 200710001049A CN 100510021 C CN100510021 C CN 100510021C
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Abstract
This invention relates to a process for separating effluent of hydrogenation reaction. The method comprises: (1) sending the effluent of hydrogenation reaction into a high-temperature high-pressure separator; (2) cooling the separated gas phase, and sending into a medium-temeprature high-pressure separator; (3) cooling the separated gas phase, sending into a low-temeprature high-pressure separator, and utilizing the separated gas phase as circulating H2; (4) setting a heat exchange column, sending the liquid phase from the high-temperature high-pressure separator into the heat exchange column from the bottom, sending the liquid phase from the medium-temeprature high-pressure separator into the heat exchange column from the middle, sending the liquid phase from the low-temeprature high-pressure separator into the heat exchange column from the overhead, steam-stripping the liquid phase from the column bottom, cooling the gas phase from the column overhead, and separating in a gas-liquid separator. The method has such advantages as simple process, few high-pressure equipments, small area of heat exchange equipment, low cooling load, and high energy recovery rate, and is suitable for a variety of hydrogenation processes by using heat separation.
Description
Technical field
The present invention relates to a kind of hydrogenation reaction effluent thermal separation flow process, promptly adopt the separation method, the particularly separation method of hydrocracking process reaction effluent of the hydrogenation process reaction effluent of thermal separation.
Background technology
In the world wide crude quality worse and worse, the character that obtains product by crude oil processing is the phase strain differential also; And, the specification of quality of various petroleum productss is progressively improved along with the increasingly stringent of environmental regulation.Hydrogenation technique provides the important processing means of high quality petroleum products, therefore paid much attention to, range of application more and more widely, processing power improves year by year.According to the difference of feedstock property and product requirement, can adopt dissimilar hydrogenation technique processes, present widely used hydrogenation technique comprises processes such as hydrotreatment, hydrofining, hydro-upgrading, hydrocracking, hydrogenation pour point depression.
The hydrogenation technique flow process mainly comprises reactive moieties and separate part.The hydrogenation reaction part mainly comprises reactor and heating installation and power-equipment etc., and hydrogenation reaction effluent is the complex mixture of multiple cut, therefore needs separate part to carry out material and product separation.Separate part generally comprises separator, interchanger, water cooler, stripping tower, separation column etc.Hydrogenation reaction is generally carried out under High Temperature High Pressure, and reaction effluent is high temperature, high pressure mixing logistics, and the separation process design of this High Temperature High Pressure mixture flow all has material impact to facility investment, energy recovery and utilization, process cost etc.
A kind of typical process of existing hydrogenation reaction effluent separation system as shown in Figure 2, the high-temperature and high-pressure hydrogenation reaction effluent enters high pressure hot separator, enters thermal low-pressure separators after the step-down of high pressure hot separator liquid phase; The gas phase of high pressure hot separator through the interchanger heat exchange to the certain temperature with after water filling mixes, enter cold high pressure separator through the air-cooler cooling, after the gas phase treatment of cold high pressure separator as recycle hydrogen, cold high pressure separator oil phase and thermal low-pressure separators vapor condensation thing are mixed into the cold low separator, gas phase after the separation is as hydrogen-rich gas, further recover hydrogen after the desulfurization.Enter stripping tower respectively with the low branch liquid phase of heat after the liquid phase heat exchange after the separation.This sepn process flow process complexity, the table of equipment position is more, and big and energy recovery of cooling load and utilization ratio are lower.
USP5,164,070 has proposed a kind of recovery method of hydrocracking process product, hydrocarbon raw material enters hydrocracking reactor and reacts, reacted logistics enters first stripping tower, the hydrocarbon gas part that wherein contains a large amount of hydrogen sulfide is discharged from return tank of top of the tower, and petroleum naphtha is extracted out as side line; The heavy ends of first stripping tower bottom enters the product separation column and carries out fractionation, top portion distilled petroleum naphtha and first stripping tower side line extract out petroleum naphtha together enter second stripping tower and carry out further stripping, tell C from cat head
4 -Hydrocarbon gas, naphtha fraction enters a naphtha splitter again, is divided into light, heavy naphtha product; The product separation column fractionates out kerosene and diesel oil, and unconverted oil enters a further fractionation of vacuum fractionation tower again at the bottom of the tower.This separation process complexity, required equipment is many, does not also consider energy recovery and utilizes problem.
USP4,159,937 have proposed a kind of separation method of isocrackate, through the resulting gas-liquid mixed product of hydrocracking, adopt multistage to fractionate out the method for various isocrackates.The gas-liquid mixed product at first enters a high pressure hot separator, High Temperature High Pressure (399 ℃, carry out gas-liquid separation under 15MPa), wherein liquid phase enter a hot flash tank of low pressure (396 ℃, 1.7MPa) carry out flash distillation, obtain two kinds of products of gas-liquid; And the high pressure hot separator gas phase enters cold high pressure separator by after the condenser condenses, isolates the gas that is rich in hydrogen; The low gas that divides of heat enters flash tank again with the liquid phase of coming out from cold high pressure separator after the condensation cooling, separate down at lower pressure (2.0MPa).The weak point of this separation process is that energy recovery and utilization ratio are lower.
USP6,096,191 propose a kind of method of hydrocracking reaction thermal utilization, this method uses hydrocracking recycle hydrogen as gas stripping gas, gas stripping column is operated under high temperature, high pressure,＜371 ℃ cut is all partly extracted further separation out from stripping, and gas stripping column is come out〉371 ℃ of all or part of reactors that loop back of liquid hydrocarbon, thereby effectively utilize reaction heat, reduce the required energy of raw material preheating.Though this method utilizes reaction effluent that recycle hydrogen is heated, and has utilized reaction heat, total heat utilization ratio is lower.
CN98112925.0, CN98112915.3, CN02114456.7 etc. disclose the hydrocarbons hydrogenation conversion or the hydrotreatment process generates the oil separating method, by adopting a plurality of gas-liquid separators, realize improving C with the hydrocarbon gas in the further absorption extraction of the liquid hydrocarbon system in the separation system
3 +The rate of recovery of hydrocarbon, but separation system is comparatively complicated, and do not relate to the problem of heat recovery and utilization.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of separation method of hydrogenation reaction effluent, the inventive method have flow process simple, reduce number of devices, heat recovery and utilization rate advantages of higher.
Hydrogenation reaction effluent separation method of the present invention comprises following content:
(1) hydrogenation reaction effluent enters high pressure hot separator, and the service temperature of high pressure hot separator is 180～400 ℃, is preferably 200～380 ℃;
(2) enter after the gas phase heat exchange cooling that high pressure hot separator is told in warm high-pressure separator, the service temperature of middle temperature high-pressure separator is 140～180 ℃, is preferably 145～155 ℃;
(3) enter cold high pressure separator after the gas phase cooling that warm high-pressure separator is told in, the gas phase that cold high pressure separator is told is a recycle hydrogen, and the service temperature of cold high pressure separator is 38～65 ℃, preferred 45～55 ℃;
(4) heat exchange columns is set, heat exchange columns is provided with 5～30 blocks of theoretical trays, 10～15 blocks of theoretical trays preferably are set, the isolated liquid phase of high pressure hot separator in above-mentioned (1) enters heat exchange columns from the bottom, the isolated liquid phase of middle temperature high-pressure separator in above-mentioned (2) enters heat exchange columns from the middle part, and the isolated hydrocarbon liquid phase of cold high pressure separator in above-mentioned (3) enters heat exchange columns from the top;
(5) working pressure of heat exchange columns is 0.5～10.5MPa, be preferably 1.0～6.5MPa, the heat exchange columns column bottom temperature is 180～400 ℃, be preferably 200～380 ℃, the heat exchange columns bottom is drawn liquid phase material and is further handled, as comprising stripping processing or fractionation processing etc., the hydrogen rich gas phase materials that discharge at the heat exchange columns top is further handled or is utilized.Aforesaid operations process concrete operations condition can be determined by the factors such as Technology that those skilled in the art press feedstock property, processing purpose and employing.
The working pressure of above-mentioned high pressure hot separator, middle temperature high-pressure separator and cold high pressure separator is consistent with reacting system pressure, the pressure-losses when having only logistics to pass through equipment.
In the flow for separating outflow from hydrogenation reaction of the present invention, because heat exchange columns mainly is to be used for direct heat exchange, its this required number of theoretical plate is less, can adopt tray column, also can adopt packing tower.The isolated hydrocarbon liquid phase of cold high pressure separator directly enters the heat exchange columns cat head, the isolated liquid phase of high pressure hot separator enters heat exchange columns from heat exchange columns column plate bottom, also can enter heat exchange columns by 1～5 theoretical stage from the heat exchange columns bottom, the isolated liquid phase of middle temperature high-pressure separator is introduced heat exchange columns from heat exchange columns middle part suitable location.After can cooling, the gaseous phase materials that the heat exchange cat head is discharged enters the cold low separator.The diameter of heat exchange columns can be according to entering heat exchange columns logistics flux and character, determine by the design of this area general knowledge, concerning the inventive method, because entering most materials of heat exchange columns discharges with liquid form at the bottom of tower, the vapour phase of heat exchange columns middle and upper part load is lower, can adopt therefore that lower diameter is big, the less change tower diameter heat exchange columns structure of upper diameter.
Hydrogenation reaction effluent can be lowered the temperature with other logistics heat exchange before entering high pressure hot separator, the heat transfer process of this heat transfer process and the isolated gaseous stream of high pressure hot separator, all are the processes of utilizing of hydrogenation reaction effluent heat, for example can carry out heat exchange with the reaction raw materials in the native system.Usually contain materials such as hydrogen sulfide that hydrogenation reaction generates and ammonia in the hydrogenation reaction effluent, for preventing these substance reaction crystallization occluding device and pipelines, generally need to inject suitable quantity of water in the isolated gaseous stream of middle temperature high-pressure separator, water injection rate is determined according to the content of hydrogen sulfide in the logistics and ammonia.In the cooling of telling gas phase of warm high-pressure separator generally adopt air-cooler or water recirculator, also can adopt two kinds of type of cooling combinations.In the potential temperature of the isolated gaseous stream of warm high-pressure separator and heat exchange cat head gaseous stream lower, this portion of energy generally can not be recycled.
The inventive method can be used for various hydrogenation processes, as processes such as hydrotreatment, hydrofining, hydro-upgrading, hydrocracking, hydrogenation pour point depressions, is specially adapted to hydrocracking process.
Compared with prior art, hydrogenation reaction effluent separation method of the present invention has that flow process is simple, reduce high-tension apparatus platform position, the heat interchanging area of heat-exchange equipment significantly reduces, cooling load reduces and energy recovery utilization ratio advantages of higher.
Description of drawings
Fig. 1 is a kind of idiographic flow synoptic diagram of hydrogenation reaction effluent separation method of the present invention;
Fig. 2 is existing a kind of typical process synoptic diagram of hydrogenation reaction effluent separation method.
Wherein: 1-high pressure hot separator, warm high-pressure separator among the 2-, 3-cold high pressure separator, the 4-heat exchange columns, 5-cold low separator A, the hot high score gas of 6-interchanger A, the hot high score gas of 7-air-cooler, 8-hydrogen-rich gas water cooler A, 9-water filling, the 10-recycle hydrogen, 11-cold low separator A hydrogen-rich gas, 12-cold low separator A lime set, the charging of 13-stripping tower, 14-thermal low-pressure separators, 15-cold low separator B, the hot high score gas of 16-interchanger B, the low gas water cooler B that divides of 17-heat.
Embodiment
Further specify hydrogenation reaction effluent separation method detailed process of the present invention below in conjunction with drawings and Examples, and with the effect comparison of existing separate mode.
A kind of canonical process of existing hydrogenation effluent separation system as shown in Figure 2, the high-temperature and high-pressure hydrogenation reaction effluent enters high pressure hot separator 1, enter thermal low-pressure separators 14 after the high pressure hot separator 1 liquid phase step-down, thermal low-pressure separators 14 liquid phases are mixed as stripping tower charging 13 with cold low separator 15 lime sets after heat exchange.The gas phase warp of high pressure hot separator 1 and hot high score gas interchanger A6 heat exchange cooling divide hydrocarbon liquid phase interchanger B16 further heat exchange cooling with low again, mix through air-cooler with injection water 9 then and further cool off, and enter cold high pressure separator 3.The gas phase of cold high pressure separator 3 treated processing such as () depriving hydrogen sulphides back is as recycle hydrogen 10.Cold high pressure separator 3 oil phases mix through water cooler B17 phlegma with thermal low-pressure separators 14 gaseous streams, enter cold low separator B15 then and carry out gas-liquid separation.Gas phase after cold low separator B15 separates enters cold low separator A5 after water cooler A8 cooling, the liquid phase after cold low separator B15 separates heats up back and thermal low-pressure separators liquid-phase mixing as stripping tower charging 13 through hot high score gas interchanger B16 heat exchange.The gas phase cold low separator A hydrogen-rich gas 11 of cold low separator A5 and cold low separator lime set 12 are further handled or are utilized.
Hydrogenation effluent separation system of the present invention is improved on above-mentioned existing procedure basis, as shown in Figure 1, has saved high pressure heat exchanger B16, water cooler B17, thermal low-pressure separators 14 and cold low separator B15, has increased middle temperature high-pressure separator 2 and heat exchange columns 4.Concrete separation process is: the high-temperature and high-pressure hydrogenation reaction effluent enters high pressure hot separator 1.Warm high-pressure separator 2 during the gas phase of high pressure hot separator 1 enters after lowering the temperature with interchanger A6 heat exchange, in warm high-pressure separator 2 isolated gas phases with inject water 9 and mix after air-cooler 7 further cools off, enter cold high pressure separator 3 then, the gas phase treatment of cold high pressure separator 3 processing such as () depriving hydrogen sulphides back is as recycle hydrogen 10.Enter the bottom of heat exchange columns 4 after the high pressure hot separator 1 liquid phase step-down, middle temperature high-pressure separator 2 isolated liquid phases enter the middle part of heat exchange columns 4, and cold high pressure separator 3 isolated hydrocarbon liquid phases enter the top of heat exchange columns 4.Heat exchange columns 4 top discharge gas further enter cold low separator A5 after the cooling through water cooler A8, and cold low separator A5 isolates cold low separator A hydrogen-rich gas 11 and cold low separator A lime set 12 is further handled or utilization.The hydrogenation liquid product that discharge heat exchange columns 4 bottoms is as stripping tower charging 13.
From above-mentioned contrast as can be seen, the inventive method has reduced high pressure heat exchanger 16, thermal low-pressure separators 14, cold low separator B15 and water cooler B17, warm high-pressure separator 2 and heat exchange columns 4 in the increase, and number of devices reduces, and separation process is simplified.High pressure heat exchanger is cost height in the native system, the equipment of easy care not, and the cyclone separator arrangement that the present invention uses is simple, is easy to safeguard.In addition, though all use air-cooler (high pressure) in the present invention and the prior art, because heat exchange load reduces greatly, so the load of high-pressure air water cooler reduces greatly, and equipment cost and the maintenance cost brought thus reduce greatly.In the inventive method, will have in the method a part of unrenewable heat now and fully recycle, adopt the heat exchange mode of heat exchange columns direct contact type simultaneously, improve the recovery utilization rate of heat greatly, reduce calorific loss.
Below by embodiment with certain 150 * 10
4Hydrogenation reaction effluent adopts the present invention and existing scheme to compare in the t/a hydrocracking process, further specifies the present invention program's technique effect.
In embodiment 1 and the comparative example 1, hydrocracking reaction effluent temperature after preliminary heat exchange is 288 ℃, and pressure is 16.3MPa, and flow is 335830kg/h, and enthalpy is 101970KW.
Among the embodiment 1, high pressure hot separator 1 service temperature is 288 ℃, and the thermal load of interchanger A6 is 22612KW, and the service temperature of middle temperature high-pressure separator 2 is 166 ℃, air-cooler 7 thermal loads are 17719KW (unavailable heat), and the service temperature of cold high pressure separator 3 is 49 ℃.Heat exchange columns 4 adopts 15 blocks of theoretical trays, and the opening for feed of three kinds of logistics is separately positioned on top, middle part (the 9th theoretical stage place) and bottom, and the temperature of the stripping tower charging 13 that discharge heat exchange columns 4 bottoms is 259.7 ℃, and pressure is 4.5MPa.Cold low separator A5 service temperature is 40 ℃, and water cooler A8 thermal load is 80KW (unavailable heat).
In the comparative example 1, the service temperature of high pressure hot separator 1 is 288 ℃, and the thermal load of interchanger A6 is 16041KW, and interchanger B16 thermal load is 6571KW.Thermal low-pressure separators 14 service temperatures are 288 ℃, and pressure is 2.6MPa.Air-cooler 7 thermal loads are 20694KW (unavailable heat), and the service temperature of cold high pressure separator 3 is 49 ℃.Water cooler A8 thermal load is 37KW (unavailable heat), and water cooler B17 thermal load is 2351KW (unavailable heat), and the service temperature of cold low separator B15 is 49 ℃, and cold low separator A5 service temperature is 40 ℃, pressure 1.5MPa.Stripping tower charging 13 temperature are 260.3 ℃, and pressure is 2.6MPa.
The difference (is benchmark with the Comparative Examples) of both aspects such as energy utilization, equipment, material is described below by correlation data.As can be seen from the comparison result, compare with existing method, advantages such as the inventive method has the table of equipment position and load reduces, the water cooler load reduces greatly, recyclable heat improves greatly, other material data is basic identical simultaneously, does not influence the normal running of technological process.
The contrast of table 1 water cooler load
| Project | Comparative example 1 | |
| High pressure hot separator gas phase cooling (7-air-cooler), KW | Benchmark | Benchmark-2975 |
| Thermal low-pressure separators gas phase cooling (17-water cooler B), KW | Benchmark | Benchmark-2351 |
| Cold low separator gas phase cooling (8-water cooler A), KW | Benchmark | Benchmark+43 |
| Amount to | Benchmark | Benchmark-5283 |
The recyclable heat contrast of table 2
| Project | Comparative example 1 | |
| Recoverable energy, KW | Benchmark | Benchmark+6571 |
| The reaction heating furnace thermal load, KW | Benchmark | Benchmark-6571 |
Table 3 number of devices and scale contrast
| Project | Comparative example 1 | |
| The 7-air-cooler | ||
| Specification, m | 10.5×3 | 10.5×3 |
| Quantity, |
8 | 8 |
| Heat interchanging area, m 2 | 1775 | 1497 |
| Power of fan, kw | 30 | 30 |
| Warm high-pressure separator among the 2-, mm | Do not have | Φ2400×5650 |
| The 14-thermal low-pressure separators, mm | Φ3000×7680 | Do not have |
| The 3-cold high pressure separator, mm | Φ3200×7950 | Φ3200×7960 |
| 15-cold low separator B | Φ2800×7660 | Do not have |
| The 4-heat exchange columns | Do not have | 15 blocks of theoretical trays |
| 17-thermal low-pressure separators gas phase water cooler B | Do not have | |
| Specification, m | 10.5×1.5 | / |
| Quantity, |
2 | / |
| Heat interchanging area, m 2 | 112 | / |
| Power of fan, |
11 | / |
| 16-cold low separator oil heat exchanger B | Do not have | |
| Specification, mm | DFU1000×6000 | / |
| Heat interchanging area, m 2 | 350 | / |
| 8-cold low separator gas phase water cooler A | ||
| Specification, mm | AES400×4500 | AES400×4500 |
| Heat interchanging area, m 2 | 29 | 29 |
Table 4 recycle hydrogen purity and flow contrast
| Project | Comparative example 1 | |
| The recycle hydrogen flow | ||
| Mass rate, kg/h | Benchmark | Benchmark+3521 |
| Molar flow, kmol/h | Benchmark | Benchmark+50 |
| Molecular-weight average | Benchmark | Benchmark+0.25 |
| Recycle hydrogen is formed, (v) % | ||
| H 2 | Benchmark | Benchmark-0.43 |
| H 2S | Benchmark | Benchmark+0.04 |
| C1 | Benchmark | Benchmark+0.01 |
| C2 | Benchmark | Benchmark+0.02 |
| C3 | Benchmark | Benchmark+0.07 |
| i-C4 | Benchmark | Benchmark+0.11 |
| n-C4 | Benchmark | Benchmark+0.05 |
| H 2O | Benchmark | Benchmark+0 |
| C5 + | Benchmark | Benchmark+0.13 |
Table 5 cold low separator gas phase 11 purity and flow
| Project | Comparative example 1 | |
| Light pressure separator gas phase flow | ||
| Mass rate, kg/h | Benchmark | Benchmark-182 |
| Molar flow, kmol/h | Benchmark | Benchmark-22 |
| The low gas that divides is formed, (v) % | ||
| H 2 | Benchmark | Benchmark-0.09 |
| H 2S | Benchmark | Benchmark+0.97 |
| C1 | Benchmark | Benchmark-0.14 |
| C2 | Benchmark | Benchmark+0.32 |
| C3 | Benchmark | Benchmark-0.13 |
| i-C4 | Benchmark | Benchmark-0.18 |
| n-C4 | Benchmark | Benchmark-0.04 |
| H 2O | Benchmark | Benchmark+0 |
| C5 + | Benchmark | Benchmark-0.71 |
The contrast of table 6 hydrogen balance
| Project | Comparative example 1 | |
| From reaction product hydrogen sum, kg/h | 23736.8 | 23736.8 |
| Recycle hydrogen is taken away hydrogen, kg/h | 23062 | 23034 |
| The low band of gas that divides is walked hydrogen, kg/h | 599 | 565 |
| The stripping tower strip is walked hydrogen, kg/h | 75.8 | 137.8 |
H in the charging 13 of table 7 stripping tower
2S measures contrast
| Project | Comparative example 1 | Embodiment 1 |
| H 2S，kg/h | 476.9 | 167.3 |
Below by embodiment with certain 150 * 10
4Hydrogenation reaction effluent adopts the present invention and existing scheme to compare (flowsheeting software PRO II calculation result) in the t/a charking full distillate oil hydrogenation modifying process, further specifies the present invention program's technique effect.
In embodiment 2 and the comparative example 2, hydro-upgrading reaction effluent temperature after preliminary heat exchange is 350 ℃, and pressure is 8.5MPa, and flow is 235600kg/h, and enthalpy is 72500KW.
Among the embodiment 2, the service temperature of high pressure hot separator 1 is 350 ℃, and the thermal load of interchanger A6 is 20400KW, and middle temperature high-pressure separator 2 service temperatures are 145 ℃, air-cooler 7 thermal loads are 11300KW (unavailable heat), and the service temperature of cold high pressure separator 3 is 50 ℃.Heat exchange columns 4 adopts 5 blocks of theoretical trays, and the opening for feed of three kinds of logistics is separately positioned on top, middle part (the 2nd theoretical stage place) and bottom, and stripping tower charging 13 temperature that discharge heat exchange columns 4 bottoms are 315 ℃, and pressure is 1.5MPa.Cold low separator A5 service temperature is 40 ℃, and water cooler A8 thermal load is 70KW (unavailable heat).
In the comparative example 2, high pressure hot separator 1 service temperature is 350 ℃, and the thermal load of interchanger A6 is 15300KW, and interchanger B16 thermal load is 5100KW.Thermal low-pressure separators 14 service temperatures are 350 ℃, and pressure is 2.6MPa.Air-cooler 7 thermal loads are 15200KW (unavailable heat), and the service temperature of cold high pressure separator 3 is 50 ℃.Water cooler A8 thermal load is 25KW (unavailable heat), and water cooler B17 thermal load is 2100KW (unavailable heat), and the service temperature of cold low separator B15 is 50 ℃, and cold low separator A5 service temperature is 40 ℃, pressure 1.5MPa.Stripping tower charging 13 temperature are 315 ℃, and pressure is 1.5MPa.
The difference (is benchmark with the Comparative Examples) of both aspects such as energy utilization, equipment, material is described below by correlation data.As can be seen from the comparison result, compare with existing method, the inventive method has advantages such as reduce with load the table of equipment position, the water cooler load reduces greatly, recyclable heat improves greatly.
The contrast of table 8 water cooler load
| Project | Comparative example 2 | |
| High pressure hot separator gas phase cooling (7-air-cooler), KW | Benchmark | Benchmark-3900 |
| Thermal low-pressure separators gas phase cooling (17-water cooler B), KW | Benchmark | Benchmark-2100 |
| Cold low separator gas phase cooling (8-water cooler A), KW | Benchmark | Benchmark+45 |
| Amount to | Benchmark | Benchmark-5955 |
The recyclable heat contrast of table 9
| Project | Comparative example 2 | |
| Recoverable energy, KW | Benchmark | Benchmark+5100 |
| The reaction heating furnace thermal load, KW | Benchmark | Benchmark-5100 |
Table 10 number of devices and scale contrast
| Project | Comparative example 2 | |
| The 7-air-cooler | ||
| Specification, m | 10.5×3 | 10.5×3 |
| Quantity, |
6 | 6 |
| Heat interchanging area, m 2 | 1316 | 1122 |
| Power of fan, kw | 25 | 25 |
| Warm high-pressure separator among the 2-, mm | Do not have | Φ2160×5090 |
| The 14-thermal low-pressure separators, mm | Φ2700×6900 | Do not have |
| The 3-cold high pressure separator, mm | Φ2700×6350 | Φ2700×6350 |
| 15-cold low separator B | Φ2200×6100 | Do not have |
| The 4-heat exchange columns | Do not have | 5 blocks of theoretical trays |
| 17-thermal low-pressure separators gas phase water cooler B | Do not have | |
| Specification, m | 10.5×1.5 | / |
| Quantity, |
2 | / |
| Heat interchanging area, m 2 | 90 | / |
| Power of fan, |
9 | / |
| 16-cold low separator oil heat exchanger B | Do not have | |
| Specification, mm | DFU1000×6000 | / |
| Heat interchanging area, m 2 | 280 | / |
| 8-cold low separator gas phase water cooler A | ||
| Specification, mm | AES400×4500 | AES400×4500 |
| Heat interchanging area, m 2 | 22 | 22 |
Claims (10)
1, a kind of flow for separating outflow from hydrogenation reaction comprises following content:
(1) hydrogenation reaction effluent enters high pressure hot separator, and the service temperature of high pressure hot separator is 180～400 ℃;
(2) enter after the gas phase heat exchange cooling that high pressure hot separator is told in warm high-pressure separator, the service temperature of middle temperature high-pressure separator is 140～180 ℃;
(3) enter cold high pressure separator after the gas phase cooling that warm high-pressure separator is told in, the gas phase that cold high pressure separator is told is a recycle hydrogen, and the service temperature of cold high pressure separator is 38～65 ℃;
(4) heat exchange columns is set, heat exchange columns is provided with 5～30 blocks of theoretical trays, the isolated liquid phase of high pressure hot separator in above-mentioned (1) enters heat exchange columns from the bottom, the isolated liquid phase of middle temperature high-pressure separator in above-mentioned (2) enters heat exchange columns from the middle part, and the isolated hydrocarbon liquid phase of cold high pressure separator in above-mentioned (3) enters heat exchange columns from the top;
(5) working pressure of heat exchange columns is 0.5～10.5MPa, and the heat exchange columns column bottom temperature is 180～400 ℃, and the heat exchange columns bottom is drawn liquid phase material and further handled, and the hydrogen rich gas phase materials that discharge at the heat exchange columns top is further handled or utilized.
2, according to the described separation process of claim 1, it is characterized in that: the service temperature of described high pressure hot separator is 200～380 ℃.
3, according to the described separation process of claim 1, it is characterized in that: the service temperature of warm high-pressure separator is 145～155 ℃ in described.
4, according to the described separation process of claim 1, it is characterized in that: the service temperature of described cold high pressure separator is 45～55 ℃.
5, according to the described separation process of claim 1, it is characterized in that: described heat exchange columns is provided with 10～15 blocks of theoretical trays.
6, according to the described separation process of claim 1, it is characterized in that: the working pressure of described heat exchange columns is 1.0～6.5MPa.
7, according to claim 1 or 6 described separation process, it is characterized in that: described heat exchange columns column bottom temperature is 200～380 ℃.
8, according to claim 1 or 6 described separation process, it is characterized in that: described heat exchange columns bottom is drawn liquid phase material and is comprised that stripping is handled or fractionation is handled.
9, according to the described separation process of claim 1, it is characterized in that: the working pressure of described high pressure hot separator, middle temperature high-pressure separator and cold high pressure separator is consistent with reacting system pressure.
10, according to the described separation process of claim 1, it is characterized in that: heat exchange was lowered the temperature before described hydrogenation reaction effluent entered high pressure hot separator, injected water in the isolated gaseous stream of middle temperature high-pressure separator.
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|---|---|---|---|
| CNB2007100010499A CN100510021C (en) | 2007-01-22 | 2007-01-22 | Flow for separating outflow from hydrogenation reaction |
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| CN103131466A (en) * | 2011-11-25 | 2013-06-05 | 中国石油天然气股份有限公司 | Aromatic hydrocarbon-rich wax oil hydrotreating method |
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