阅读说明：本技术 一种降低蒸汽裂解装置丙烯机火炬排放量的方法和装置 (A kind of method and apparatus reducing steam cracking device propylene machine flare discharge amount ) 是由 彭勃 刘蒙 王振维 赵百仁 李广华 于 2018-05-24 设计创作，主要内容包括：本发明属于化工领域,涉及一种降低蒸汽裂解装置丙烯机火炬排放量的方法和装置。该方法包括：将原料碳三进行预处理净化,然后减压、加热气化,回收原料碳三的冷量,加热气化后的原料碳三经升压升温后排出。本发明可以显著降低丙烯机功率,降低制冷系统总能耗,并且降低蒸汽裂解装置火炬排放量。(The invention belongs to chemical fields, are related to a kind of method and apparatus for reducing steam cracking device propylene machine flare discharge amount.This method comprises: material carbon three is carried out pretreatment purification, then decompression, heating and gasifying is recycled the cooling capacity of material carbon three, is discharged after the boosted heating of material carbon three after heating and gasifying.Propylene machine power can be significantly reduced in the present invention, reduces refrigeration system total energy consumption, and reduce steam cracking device flare discharge amount.)

1. a kind of method for reducing steam cracking device propylene machine flare discharge amount, which is characterized in that this method comprises: by raw material Carbon three carries out pretreatment purification, then decompression, heating and gasifying, recycles the cooling capacity of material carbon three, the material carbon three after heating and gasifying It is discharged after boosted heating.

2. according to the method described in claim 1, wherein, the method for the pretreatment purification includes dehydration and de- solid impurity.

3. according to the method described in claim 1, wherein, the decompression is by the pressure reduction of material carbon three to 10- 700kPaG。

4. according to the method described in claim 1, wherein, the cryogen level that the cooling capacity of the recycling material carbon three provides is -40 DEG C to 40 DEG C, for supplying at least one cryogen user, the cryogen user has identical or different cryogen level demand.

5. the condition of the boosting heating is that pressure rises to 450-1200kPaG according to the method described in claim 1, wherein, Temperature rises to 25-85 DEG C；Preferably, boosting is realized by compressor, and the material carbon three after heating and gasifying is directly entered compressor, Or compressor is entered with 1 DEG C or more of the degree of superheat via superheater.

6. according to the method described in claim 1, material carbon three is by repeatedly decompression, to recycle the cooling capacity of different levels, heating The corresponding pressure level that material carbon three after gasification respectively enters compressor is compressed.

7. according to the method described in claim 1, wherein, the method includes one of following three kinds of modes:

Mode one:

Material carbon three removes moisture through coalescer and drier, again by filter removing solid impurity, is then divided into two strands of objects Stream,

First strand of logistics heated after depressurisation gasifies to the first level, recycles the first level cooling capacity, obtains gas phase I-1 and liquid phase I-1, The gas phase I-1 goes to two sections of compressor, and heated after depressurisation gasifies the liquid phase I-1 again, recycles the second level cooling capacity, obtains Gas phase I-2 and liquid phase I-2, the gas phase I-2 enter two sections of compressor after going to one section of compressor compression；

Bypass gasifier is gone to after second burst of logistics decompression, gas phase II is obtained and liquid phase II, the gas phase II goes to compressor two Section；

Compressor second stage exit gas is sent to gas pyrolysis furnace；

Liquid cracking furnace is sent to through pressurization after the liquid phase I-2 and liquid phase II merging；

Mode two:

Material carbon three removes moisture through coalescer and drier, again by filter removing solid impurity, is then divided into three strands of objects Stream；

First strand of logistics heated after depressurisation gasifies to the first level, recycles the first level cooling capacity, obtains gas phase A and liquid phase A, described Gas phase A goes to knockout drum；

Knockout drum is gone to after second burst of logistics decompression；

Bypass gasifier is gone to after third stock logistics decompression, gas phase B is obtained and liquid phase B, the gas phase B goes to knockout drum；

The isolated gas phase C of the knockout drum and liquid phase C, the gas phase C go to two sections of compressor, and the liquid phase C is through subtracting Pressure and heating and gasifying recycle the second level cooling capacity, gas phase D and liquid phase D are obtained, after the gas phase D goes to one section of compressor compression Into two sections of compressor, compressor second stage exit gas is sent to gas pyrolysis furnace；

The liquid phase A, the liquid phase B and the liquid phase D through pressurization are sent to liquid cracking furnace after merging；

Mode three:

Material carbon three removes moisture through coalescer and drier, again by filter removing solid impurity, receives by propane cryogen After collecting tank, obtains gas phase A and liquid phase A, the liquid phase A enter an open type refrigeration cycle and recycle cooling capacity step by step；

Every level-one cold recovery includes that one liquid phase stream heated after depressurisation gasifies to this level, recycles this level cooling capacity, is entered This section of suction tank, another strand of liquid phase stream are directly entered this section of suction tank, isolated gas phase and liquid phase in this section of suction tank, The gas phase goes to next stage compressor after going to this section of compressor, is ultimately destined for afterbody compressor, and the liquid phase enters Next stage cold recovery；

Final stage compressor outlet gas enters the propane cryogen collecting tank via compressor water cooler；The propane cryogen Having heaters is arranged in collecting tank, for removing the light component of accumulation in a device；

The corresponding suction tank of first segment compressor is provided with cryogenic fluid pump, is pressurized to unvaporized heavy cryogen, after recycling cooling capacity It is sent into gas pyrolysis furnace；

Gas-phase carbon three is extracted out between compressor section, is sent into gas pyrolysis furnace after recycling cooling capacity.

8. a kind of device for reducing steam cracking device propylene machine flare discharge amount, which is characterized in that the device includes:

Clean unit is pre-processed, for material carbon three to be carried out pretreatment purification；

Decompressing unit, for depressurizing purified material carbon three；

Gasification and cryogen subscriber unit carry out heating and gasifying for the material carbon three after depressurizing, while recycling material carbon three Cooling capacity；

Boosting heating unit, for the material carbon three after heating and gasifying to be carried out boosting heating.

9. device according to claim 8, wherein when gasification is not enough to gasify whole material carbons three with cryogen subscriber unit When, which further includes heating by-pass unit.

Technical field

The present invention relates to chemical fields, more particularly, to a kind of method for reducing steam cracking device flare discharge amount And device.

Background technique

As the raw material of preparing ethylene by steam cracking becomes more diverse, since light component raw material has yield of ethene height, price Cheap, the features such as energy consumption of unit product is low, thus the light components such as ethane, propane, butane hydro carbons increasingly become cracking dress The important source material set.How according to the physicochemical characteristics of light raw material more sufficiently, more reasonably utilize light hydrocarbon feedstocks, be to mention from now on The key of high ethylene unit benefit.

Three raw material of carbon is usually transported to steam cracking device in the form of room temperature (20 DEG C), liquid, when as cracking stock, It is 700kPaG or so that pyrolysis furnace entrance, which requires (1) pressure, and (2) phase is gas phase.Carbon three needs to be heated to 21 at this pressure DEG C or more can all gasify, for guarantee operation stability, need carbon three being superheated to 60 DEG C.

In preparing ethylene by steam cracking device, the preferred heat medium of low temperature position is usually chilled water (chw), 100 tons of gasification/small When three raw material of carbon, need 643.8 ton/hours of chilled water (chw) (83 DEG C of entrance, export 70 DEG C).These chilled water (chw)s are not if used propane Gasification cooling needs then to need to consume 838 ton/hours of recirculated water using circulating water.When whole device raw material is whole lighter When, the chilling water balance of full device is nervous, and excessive chilling water consumption will affect chilling water balance, need when in short supply using low It presses steam to replace chilled water (chw), causes significant wastage.

Can flare discharge device be the essential safety dumping combustion plant of ethylene cracker, run well pair Due to interruption to switch to disaster most important for anti-locking apparatus when there are the emergencies such as fire or power-off for device.But torch is arranged Putting device itself, there is also great risk, and certain influence is generated to environment.Therefore, reducing flare discharge is always The target that petrochemical industry is pursued.Control of the especially torch general pipeline of steam cracking device usually by propylene machine discharge operating condition How system, be effectively reduced propylene machine power, to reduce full device flare discharge amount, has in existing apparatus capacity expansion revamping non- Often important meaning and effect.

Summary of the invention

The present inventor has found under study for action, by handling material carbon three, can recycle material carbon three Cooling capacity reduces the load of refrigeration machine, at the same time, reduces discharge of safety valve discharge amount and then reduces ethylene unit torch Discharge amount.Based on above-mentioned discovery, the present invention provides a kind of method and dress for reducing steam cracking device propylene machine flare discharge amount It sets.This method and device can reduce ethylene unit flare discharge amount while meeting downstream cleavage furnace import requirement, and show Write the circulation water consumption for reducing integrated artistic.

The first aspect of the present invention is to provide a kind of method for reducing steam cracking device propylene machine flare discharge amount, the party Method includes: that material carbon three is carried out pretreatment purification, then decompression, heating and gasifying, recycles the cooling capacity of material carbon three, heating and gasifying It is discharged after the boosted heating of material carbon three afterwards.

The second aspect of the present invention is to provide a kind of device for reducing steam cracking device propylene machine flare discharge amount, the dress It sets and includes:

Clean unit is pre-processed, for material carbon three to be carried out pretreatment purification；

Decompressing unit, for depressurizing purified material carbon three；

Cryogen subscriber unit carries out heating and gasifying with by the material carbon three after decompression, while recycling the cooling capacity of material carbon three；

Boosting heating unit, for the material carbon three after heating and gasifying to be carried out boosting heating.

Effect of the invention is: the preparing ethylene by steam cracking device based on lightweight material, with the offer of gasified raw material propane Cooling capacity can substitute part propylene cryogen, to significantly reduce propylene refrigeration compressor power.Chilling area disk oil and chilled water (chw) are not When sufficient, it is necessary to consume a large amount of chilled water (chw) heating and gasifying material carbon three, by taking 100 tons of three raw materials of carbon that gasify as an example, need 643.8 Ton/hour chilled water (chw) (83 DEG C of entrance, export 70 DEG C).These chilled water (chw)s use circulation if do not used propane gasification cooling Water is cooling, then needs to consume 838 ton/hours of recirculated water.According to the method for proposition of the invention, three raw material of carbon for the equivalent that gasifies - 40 to 19 DEG C of cooling capacity can be separately or concurrently provided.If only providing level-one cooling capacity, raw material propane only passes through full flashing.

Compared with chilled water (chw) directly heats, the present invention has the economic benefit of highly significant.Especially the present invention can not Change existing apparatus propylene refrigeration compressor, so that it may the cooling capacity for being equal to propylene level is provided, in existing apparatus capacity expansion revamping There is good application prospect in de- bottleneck.

Further, since ethylene unit flare discharge amount maximum is mainly controlled by propylene machine discharge amount, calculated, is utilized Method of the invention, the flare discharge reduction amount of steam cracking device are equivalent to the 105% of charging propane amount.This method makes the whole series Device operation is safer, and reduces the pollution to environment.

Other features and advantages of the present invention will then part of the detailed description can be specified.

Detailed description of the invention

Exemplary embodiment of the invention is described in more detail in conjunction with the accompanying drawings, it is of the invention above-mentioned and its Its purpose, feature and advantage will be apparent.

Fig. 1 is the flow chart of the embodiment of the present invention 1.

Fig. 2 is the flow chart of the embodiment of the present invention 2.

Fig. 3 is the flow chart of the embodiment of the present invention 3.

Fig. 4 is the flow chart of the embodiment of the present invention 4.

Fig. 5 is the flow chart of comparative example 1.

E1 user's gasifier 1, E2 bypass gasifier, E3 user's gasifier 2, three superheater of E4 carbon；

D0 coalescer, D1 knockout drum；DR1 drier；S1 filter；

D10 propane cryogen collecting tank, one section of suction tank of D11 propane machine, two sections of suction tanks of D12 propane machine, D13 propane machine three Section four sections of suction tank, D14 propane machine suction tanks；

E11-35 DEG C of cryogen user heat exchanger, E12-22 DEG C of cryogen user heat exchanger, E13-1 DEG C of cryogen user heat exchanger, 12 DEG C of cryogen user heat exchangers of E14, E15 propane compressor water cooler, E16 propane take off light component gasifier, E17 phase propane Superheater, E18 heavy constituent gasifier；

C1 compressor, one section of C1-I compressor, two sections of C1-II compressor, three sections of C1-III compressor, C1-IV compressor Four sections.

Specific embodiment

The preferred embodiment that the present invention will be described in more detail below with reference to accompanying drawings.Although showing the present invention in attached drawing Preferred embodiment, however, it is to be appreciated that may be realized in various forms the present invention without the embodiment party that should be illustrated here Formula is limited.On the contrary, thesing embodiments are provided so that the present invention is more thorough and complete, and can will be of the invention Range is completely communicated to those skilled in the art.

The present invention provides a kind of method for reducing steam cracking device flare discharge amount, this method comprises: by material carbon three Pretreatment purification is carried out, then decompression, heating and gasifying, recycles the cooling capacity of material carbon three, the material carbon three after heating and gasifying is through rising It is discharged after pressure heating.Gas downstream pyrolysis furnace can be entered after discharge.

According to the present invention, the effect for pre-processing purification is the moisture and solid impurity removed in raw material, avoids enter into downstream Cryogenic heat exchanger moisture or hydrocarbon hydrate frozen block.Preferably, the method for the pretreatment purification includes dehydration and de- solid impurity. Dehydration can first pass through the hydrone of coalescer removing free state, then moisture is removed in depth by drier, and the drier is for example It can be mol sieve beds.Preferably, the water content after dehydration in material carbon three is lower than 50ppm.De- solid impurity can pass through Filter realizes that the solid impurity is usually the dust carried secretly.

According to the present invention, the decompression can be realized by regulating valve, it is preferable that the decompression is by the pressure of material carbon three It is reduced to 10-700kPaG.The pressure reduction of material carbon three, temperature also reduce.

After pretreated three logistics of carbon decompression, corresponding saturation temperature is reduced.On the one hand it can make carbon three can be with Gasified in lower temperature, reduce gasification difficulty, so that carbon three is gasified using the lower heat source of temperature at this pressure, The cooling capacity of chilled water (chw) can be saved；While another aspect carbon three gasifies, the propylene of part can be replaced by recycling cooling capacity therein Cryogen reduces propylene refrigerant dosage, reduces propylene refrigeration compressor power.

The heat medium of the heating and gasifying can be 30-85 DEG C of medium, preferably device technique medium or public work Cheng Jiezhi.

The cooling capacity in material carbon three can be recycled while vaporized carbon three, temperature level can be from -40 DEG C to 40 DEG C, substitution Part propylene cryogen；For supplying at least one cryogen user, there is the cryogen user identical or different cryogen level to need It asks.At this point, material carbon three can be by repeatedly decompression, to recycle the cooling capacity of different levels, the material carbon three after heating and gasifying is distinguished Corresponding pressure level into compressor is compressed.For example, the first stage pressure in 10kPaG between 450kPaG, the second level Pressure is in 100kPaG between 800kPaG.

The pressure as needed for compressor boost to downstream of gas-phase carbon three after gasification, temperature raising meet pyrolysis furnace entrance and want It asks.

To meet downstream pressure, it is preferable that the condition of the boosting heating is that pressure rises to 450-1200kPaG, temperature liter To 25-85 DEG C.The boosting preferably realizes that the material carbon three after heating and gasifying is directly entered compressor, or warp by compressor Compressor is entered with 1 DEG C or more of the degree of superheat by superheater.

A kind of specific embodiment according to the present invention, includes the following steps, as shown in Figure 1:

(1) pretreatment of material carbon three dehydration, de- solid impurity；

(2) material carbon three depressurizes, as pressure is down to 50 to 150kPaG；

(3) three temperature of carbon after depressurizing is reduced to 12 to 28 DEG C；

(4) carbon three after depressurizing enters gasifier, and heat medium is processing medium or other public work media；

(5) gasification of carbon three can provide the cooling capacity of 12 to 28 DEG C of levels for user.

(6) three component of carbon to gasify enters compressor, is pressurized to gas pyrolysis furnace required pressure；

(7) remaining liquid heavy constituent is by entering liquid cracking furnace entrance after pump pressurization.

Method of the invention can be used for more complicated demand status, for example, the method may include following three kinds of modes One of:

Mode one (as shown in Figure 3):

Material carbon three removes moisture through coalescer and drier, again by filter removing solid impurity, is then divided into two Stock logistics,

First strand of logistics heated after depressurisation gasifies to the first level, recycles the first level cooling capacity, obtains gas phase I-1 and liquid phase I-1, the gas phase I-1 go to two sections of compressor, and heated after depressurisation gasifies the liquid phase I-1 again, recycle the second level cooling capacity, It obtains gas phase I-2 and liquid phase I-2, the gas phase I-2 enters two sections of compressor after going to one section of compressor compression；

Bypass gasifier is gone to after second burst of logistics decompression, gas phase II is obtained and liquid phase II, the gas phase II goes to compression Two sections of machine；

Compressor second stage exit gas is sent to gas pyrolysis furnace；

Liquid cracking furnace is sent to through pressurization after the liquid phase I-2 and liquid phase II merging；

Mode two (as shown in Figure 2):

Material carbon three removes moisture through coalescer and drier, again by filter removing solid impurity, is then divided into three Stock logistics；

First strand of logistics heated after depressurisation gasifies to the first level, recycles the first level cooling capacity, obtains gas phase A and liquid phase A, The gas phase A goes to knockout drum；

Knockout drum is gone to after second burst of logistics decompression；

Bypass gasifier is gone to after third stock logistics decompression, gas phase B is obtained and liquid phase B, the gas phase B goes to gas-liquid separation Tank；

The isolated gas phase C of the knockout drum and liquid phase C, the gas phase C go to two sections of compressor, the liquid phase C Through decompression and heating and gasifying, the second level cooling capacity is recycled, gas phase D is obtained and liquid phase D, the gas phase D goes to one section of compressor pressure Enter two sections of compressor after contracting, compressor second stage exit gas is sent to gas pyrolysis furnace；

The liquid phase A, the liquid phase B and the liquid phase D through pressurization are sent to liquid cracking furnace after merging；

Mode three (as shown in Figure 4):

Material carbon three removes moisture through coalescer and drier, again by filter removing solid impurity, cold by propane After agent collecting tank, obtains gas phase A and liquid phase A, the liquid phase A enter an open type refrigeration cycle and recycle cooling capacity step by step；

Every level-one cold recovery includes that one liquid phase stream heated after depressurisation gasifies to this level, recycles this level cooling capacity, Into this section of suction tank, another strand of liquid phase stream is directly entered this section of suction tank, in this section of suction tank isolated gas phase and Liquid phase, the gas phase go to next stage compressor after going to this section of compressor, are ultimately destined for afterbody compressor, the liquid phase Into next stage cold recovery；

Final stage compressor outlet gas enters the propane cryogen collecting tank via compressor water cooler；The propane Having heaters is arranged in cryogen collecting tank, for removing the light component of accumulation in a device；

The corresponding suction tank in first segment suction port of compressor is provided with cryogenic fluid pump, is pressurized to unvaporized heavy cryogen, returns Gas pyrolysis furnace is sent into after receiving cooling capacity；

Gas-phase carbon three is extracted out between compressor section, is sent into gas pyrolysis furnace after recycling cooling capacity.

Preferably, the open type refrigeration cycle includes three sections of cold recoveries.

The present invention also provides a kind of device of steam cracking device recycling three cooling capacity of material carbon, which includes:

Clean unit is pre-processed, for material carbon three to be carried out pretreatment purification；

Decompressing unit, for depressurizing purified material carbon three；

Gasification and cryogen subscriber unit carry out heating and gasifying for the material carbon three after depressurizing, while recycling material carbon Three cooling capacity；

Boosting heating unit, for the material carbon three after heating and gasifying to be carried out boosting heating.

Preferably, when gasification is not enough to gasify whole material carbons three with cryogen subscriber unit, which further includes heating By-pass unit.

Below with reference to embodiment, the present invention is further illustrated.