阅读说明：本技术 产生气体产物的方法 (Method for producing gaseous products ) 是由 S·阿梅德 T·蒙克 于 2020-02-28 设计创作，主要内容包括：本发明涉及一种用于产生气体产物(SNG)的方法,该方法包括以下步骤：a)提供进料流(FDS)的第一部分(PF1),b)提供进料流(FDS)的第二部分(PF2),c)将所述进料流(FDS)的所述第一部分(PF1)与所述进料流(FDS)的所述第二部分(PF2)合并成所述进料流(FDS),d)加热以下至少一项：iv.所述进料流(FDS)的所述第一部分(PF1),v.在步骤3之前的所述进料流(FDS)的所述第二部分(PF2),vi.在步骤c)之后的所述进料流(FDS),e)将进料流(FDS)导入反应器(RCT),f)将进料流(FDS)反应成气体产物(SNG)。为了降低投资、特别是机器的占地面积,步骤d)至少部分地通过用超音速压缩机(SCO)压缩相应的流(FDS)来进行,从而使得相应的流被加热。(The present invention relates to a method for producing a gaseous product (SNG), comprising the steps of: a) providing a first part (PF1) of a feed stream (FDS), b) providing a second part (PF2) of a feed stream (FDS), c) combining the first part (PF1) of the feed stream (FDS) with the second part (PF2) of the feed stream (FDS) into the feed stream (FDS), d) heating at least one of: the first part (PF1) of the feed stream (FDS), v the second part (PF2) of the feed stream (FDS) before step 3, vi the feed stream (FDS) after step c), e) introducing the feed stream (FDS) into a Reactor (RCT), f) reacting the feed stream (FDS) into a gaseous product (SNG). In order to reduce the investment, in particular the footprint of the machine, step d) is carried out at least partially by compressing the respective stream (FDS) with a Supersonic Compressor (SCO), so that the respective stream is heated.)

1. A method for producing a gaseous product (SNG), the method comprising the steps of:

a) providing a first portion (PF1) of a feed stream (FDS),

b) providing a second portion (PF2) of the feed stream (FDS),

c) combining the first portion (PF1) of the feed stream (FDS) with the second portion (PF2) of the feed stream (FDS) into the feed stream (FDS),

d) heating at least one of

i. The first portion (PF1) of the feed stream (FDS),

the second portion (PF2) of the feed stream (FDS) prior to step 3,

the feed stream (FDS) after step c),

e) introducing the feed stream (FDS) into a Reactor (RCT),

f) reacting the feed stream (FDS) into the gaseous product (SNG),

characterized in that step d) is carried out at least partially by compressing the respective stream (FDS) using a Supersonic Compressor (SCO), so that said respective stream is heated.

2. The method according to claim 1, wherein said first portion (PF1) of said feed stream (FDS) is heated according to step d) by compression by a Supersonic Compressor (SCO).

3. The process according to claim 1 or 2, wherein the second portion (PF2) of the feed stream (FDS) is heated upstream entering the Reactor (RCT) by heat exchange with the Reactor (RCT) and/or with the gaseous product (SNG) downstream exiting the Reactor (RCT).

4. A method according to claim 1, 2 or 3, wherein the Supersonic Compressor (SCO) is driven by a Gas Turbine (GT) generating an exhaust gas (EXG) for heating the second portion (PF2) of the feed stream (FDS).

5. The method according to at least one of claims 1, 2, 3, 4,

the first part (PF1) of the feed stream (FDS) consisting essentially of hydrocarbons (CH4),

the second portion (PF2) of the feed stream (FDS) consists essentially of water (H2O), wherein the gaseous product (SNG) consists essentially of Syngas (SYG).

6. Process according to claim 5, wherein the synthesis gas (SYG) is separated from water (H2O) and Carbon Oxides (COX) to obtain hydrogen (H2) downstream of the Reactor (RCT).

7. The method according to at least one of claims 1, 2, 3, 4,

said first portion (PF1) of said feed stream (FDS) consisting essentially of AIR (AIR),

said second portion (PF2) of said feed stream (FDS) consisting essentially of propane (C3H8),

the gaseous product (SNG) consists essentially of propylene (C3H 6).

8. The method according to claim 7, wherein said first portion (PF1) of said feed stream (FDS) is heated according to step d) by compression by a Supersonic Compressor (SCO).

9. The process according to claim 7 or 8, wherein said second portion (PF2) of the feed stream (FDS) is heated upstream entering the Reactor (RCT) by heat exchange with said first portion (PF1) of the feed stream (FDS) downstream exiting the Supersonic Compressor (SCO).

10. The method according to at least one of claims 1, 2, 3, 4,

the first portion (PF1) of the feed stream (FDS) consisting essentially of Syngas (SYG),

said second portion (PF2) of said feed stream (FDS) consisting essentially of AIR (AIR),

the gaseous product (SNG) consists essentially of ammonia (NH 3).

11. The method according to claim 10, wherein the first portion (PF1) of the feed stream (FDS) consisting essentially of Syngas (SYG) is produced by the method according to claim 7 or 5.

Technical Field

The present invention relates to a method for producing a gaseous product.

Background

In the terminology of the present invention, a supersonic compressor is a compressor comprising a rotor, wherein at least a portion of the rotor reaches mach 1, i.e. at least sonic speed, in a partial process fluid regime during standard operation of the respective compressor.

One example of a supersonic compressor is shown in US 2016/0281722 a 1.

According to the terminology of the present invention, synthesis gas or syngas is a gas mixture that is used as an intermediate for the production of gaseous products such as syngas, hydrogen or ammonia. Syngas consists primarily of hydrogen, carbon monoxide and often some carbon dioxide.

Syngas can be produced from many sources, including natural gas, coal, biomass, or virtually any hydrocarbon feedstock, by reaction with steam (steam reforming), carbon dioxide (dry reforming), or oxygen (partial oxidation).

The synthesis gas is produced mainly by a steam methane reforming process. The reaction is endothermic and therefore an external heat source must be provided to the system. Typically, the external heat is provided by a furnace. In addition, the reaction requires a pressure of 20 to 30 bar to produce the desired gaseous product.

The furnaces require a large amount of energy during operation and the costs of providing the furnaces and maintaining them are high.

Another example of large scale product gas generation is the propane dehydrogenation process. In this process, propylene is produced from propane by removing hydrogen. The reaction is carried out in a reactor in the presence of a catalyst. A feed stream of propane is heated at high temperature in a furnace and fed to a catalytic reactor for conversion to the product gas, propylene. The catalyst needs to be continuously regenerated by supplying air into the reactor.

Another example of a large scale production of gaseous products is the production of ammonia. Typically, such production plants require expensive furnaces capable of operating at high pressure levels.

Disclosure of Invention

It is an object of the present invention to provide a process for producing a gaseous product with a reduced footprint and reduced investment and operating costs.

According to the invention, a method of the aforementioned type comprising the additional features of the characterizing portion of claim 1 enables investment and operating costs to be reduced, in particular making the footprint of the installation smaller.

An advantageous feature of the present invention is that the supersonic compressor is capable of significantly increasing pressure and temperature while significantly reducing footprint compared to conventional devices.

The supersonic compression according to the present invention is particularly advantageous for simultaneously increasing the pressure and temperature of the gas feed stream so that subsequent reactions can be carried out in the reactor without the need for additional furnace operations.

In order to avoid reactions outside the reactor, a preferred embodiment provides that the first part of the feed stream for the reaction is heated by compression using a supersonic compressor. Combining at least two or several portions of the feed stream downstream of the supersonic compression of at least a portion of the feed stream avoids undesirable reactions occurring inside the supersonic compressor during the pressure and temperature increase.

Another preferred embodiment provides for heat exchange between the second portion of said feed stream entering the reactor upstream and the reactor itself or the gaseous product leaving the reactor downstream.

Another beneficial option is to use a gas turbine that produces an exhaust gas to drive the supersonic compressor, wherein the exhaust gas is used to heat the first and/or second portions of the feed stream. Thus, the thermal efficiency of the apparatus, i.e., the process, can be improved.

A preferred embodiment provides a process according to the invention, wherein said first part of said feed stream consists essentially of hydrocarbons, said second part of said feed stream consists essentially of water, and wherein the gaseous product consists essentially of synthesis gas. The synthesis gas may be separated from water and carbon oxides to obtain hydrogen downstream of the reactor, which hydrogen may be used in any subsequent process.

In another preferred embodiment of the present invention, said first portion of said feed stream consists essentially of air, said second portion of said feed stream consists essentially of propane, and said gaseous product consists essentially of propylene. The process is preferably operated such that a first portion of said feed stream is heated by compressing said air with a supersonic compressor.

To further improve thermal efficiency, the second portion of the feed stream may be heated upstream of entering the reactor by heat exchange with the first portion of the feed stream downstream of exiting the supersonic compressor.

Another preferred embodiment provides that said first portion of said feed stream consists essentially of syngas, said second portion of said feed stream consists essentially of air, and said gaseous product consists essentially of ammonia. The synthesis gas provided as said first portion of said feed stream may be produced according to the aforementioned process which provides hydrocarbons as a first portion of the feed stream and water as a second portion of said feed stream.

Drawings

The above-mentioned and other features and advantages of this invention, and the manner of attaining them, will become more apparent and the invention itself will be better understood by reference to the following description of the best mode for carrying out the invention taken in conjunction with the accompanying drawings, wherein:

figure 1 shows a schematic flow chart illustrating the basic principle of the method according to the invention,

FIGS. 2, 4 and 5 each show a schematic flow diagram illustrating the principle according to which the process according to the invention is applied to ammonia synthesis,

fig. 3 shows a schematic flow diagram of the basic principle by which the process according to the invention is applied for the dehydrogenation of propane.

Detailed Description

Fig. 1 schematically shows a flow diagram illustrating a method of producing a gaseous product SNG according to the present invention. In general, the method comprises the steps of:

a) a first portion of the feed stream FDS PF1,

b) a second portion PF2 of the feed stream FDS is provided,

c) combining the first portion PF1 of the feed stream FDS with the second portion PF2 of the feed stream FDS into the feed stream FDS,

d) heating at least one of

i. Said first portion PF1 of said feed stream FDS,

the second fraction PF2 of the feed stream FDS prior to step c),

the feed stream FDS after step 3,

e) the feed stream FDS is introduced into a reactor,

f) the feed stream FDS is reacted to the gaseous product SNG.

According to the invention, step d) is carried out by compressing the respective stream FDS using a supersonic compressor SCO, so that the respective stream is heated. The supersonic compressor SCO is pressurized and warmed in one step as required by the process. This saves process equipment and therefore reduces investment costs, especially the footprint of the machine.

Fig. 1 shows a general scheme of the invention illustrating the use of a supersonic compressor SCO to obtain the thermodynamic parameters required for the process of the method according to the invention-while fig. 2, 3 show more specific examples with more details. Fig. 2 shows a first variant of the production of the gaseous product SNG (here ammonia NH 3). The input to the process, i.e. the process, is that a first portion PF1 of the feed stream FDS, which is air, is compressed by a supersonic compressor or a common compressor CO. The second portion PF2 of the feed stream FDS is provided by natural gas NG, which may also be compressed by supersonic compressor SCO or common compressor CO. According to the invention, at least one of the two fractions PF1, PF2 of the feed stream FDS is compressed by a supersonic compressor SCO.

The illustration of fig. 2 is intended to show that at least one of the two compressors CO is provided as a supersonic compressor SCO. In this example, both compressors CO, SCO are driven by a gas turbine GT, which is supplied with fuel FUL and AIR. Driving the DRV, i.e. the gas turbine GT, produces exhaust gas EXG, which may be used in subsequent processes to heat other process fluids not shown in fig. 2.

Downstream of the compression of the natural gas NG, i.e. the second part PF2 of the feed stream FDS, is mixed with water H2O and reacted in the primary reformer RF1 to obtain synthesis gas SYG. The synthesis gas SYG is substantially a mixture of carbon oxides-in particular carbon monoxide-and hydrogen H2. The product of the first reformer RF1, i.e. the synthesis gas SYG, is reacted in the second reformer with compressed air, i.e. a first part PF1 of the feed stream FDS containing nitrogen N2 and oxygen O2. The output of the secondary reformer is essentially nitrogen N2, hydrogen H2 and carbon oxide COX, which are the feed streams FDS to be reacted in the reactor RCT downstream of the carbon oxide COX reduction module RCO. Additional compressors CO1, CO2 driven by the turbine TRB are supplied with the driving fluid DRF, wherein the reactor RCT completes the ammonia synthesis ASY. Downstream of the reactor RCT, impurities are removed from the gaseous product SNG in a separator SPR, obtaining ammonia NH 3.

Fig. 4 shows basically a similar process, with only a slight difference in the supply of water H2O to the first reformer RF 1. The water passes through the primary reformer RF1 and is heated by the reforming process. In this example, said first portion PF1 of the feed stream FDS is not compressed by the supersonic compressor SCO, but is compressed by the low-pressure compressor CLP and the subsequently provided high-pressure compressor CHP — both driven by the turbine TRB supplied with the driving fluid DRF.

Fig. 4 shows another variant of the synthesis of ammonia NH 3. In this example, only the first portion PF1 of the feed stream FDS, i.e. the AIR, is compressed by the supersonic compressor SCO. A second portion PF2 of the feed stream FDS, natural gas NG, is compressed by a common centrifugal compressor CO. The two compressors SCO, CO are driven by a drive unit DRV, i.e. a gas turbine GT supplied by AIR and fuel FUL. The additional AIR stream extracted from the output of the supersonic compressor SCO compressing the AIR is used as additional gas turbine supply AIR GTF. This hot compressed AIR improves the overall efficiency of the gas turbine GT. The exhaust EXG of the gas turbine GT is used to heat the first part PF1 of the feed stream FDS. The downstream of the process in fig. 4 is essentially the same as that shown in fig. 2 and 5.

Fig. 3 shows a schematic flow diagram of a propane dehydrogenation process using features of the present invention. The first part PF1 of the process fluid, i.e. the feed stream FDS, is AIR compressed by the supersonic compressor SCO according to the invention. The second part of the feed stream FDS, PF2, was propane C3H 8. The exhaust gas of the gas turbine GT drives the supersonic compressor SCO. The exhaust EXG of the gas turbine GT, produced by the flow of AIR AIR and fuel FUL, provides heat to the second heat exchanger HE 2. A first portion of the feed stream PF1 is heated during compression in the supersonic compressor SCO. The second part PF2 of the feed stream FDS, i.e. propane C3H8, is heated in a second heat exchanger HE2 to enter the reactor RCT together with the first part PF1 of the feed stream FDS, i.e. compressed AIR, at a temperature of about 600 ℃. The output of the reactor is, on the one hand, the exhaust EXG and, on the other hand, the deactivated catalyst DAC of the reaction. The exhaust EXG of the reactor RCT comprises hydrogen N2, oxygen O2 and carbon oxides COX, CO 2. Another output of the RCT reactor is the gaseous product SNG propylene C3H 6. To take advantage of the high temperature levels of the gaseous product SNG, the propylene C2H6 was passed through a second heat exchanger HE2 to heat a second portion of the PF2 of the feed stream FDS. The gaseous product SNG is dried in a dryer DRY and separated from impurities in a separator SPT.