# US 10,865,351 B2 · Process for producing a feed stream for a steam reforming plant

> Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt

- Number: US 10,865,351 B2
- Document ID: US10865351B2
- Status: Granted
- Kind: B2
- Application number: 16/466,761
- Filed: 2017-11-17
- Published: 2019-12-19
- Granted: 2020-12-15
- Earliest claimed: 2016-12-05
- Assignees: L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedes Georges Claude
- Applicants: L'Air Liquide, Societe Anonyme pour l'Etude et l'Exploitation des Procedes Georges Claude
- Inventors: Swatantra Kumar Shrivastava; Mrityunjoy Samaddar
- Web page: https://patentgrep.com/patent/US10865351B2

## CPC

- C10G 67/02: plural serial stages only
- C01B 3/38: using catalysts
- C10K 1/04: by cooling to condense non-gaseous materials {(C10K1/001 takes precedence)}
- C10K 3/04: reducing the carbon monoxide content {, e.g. water-gas shift [WGS]}
- B01J 23/882: and cobalt
- B01J 23/883: and nickel
- C01B 2203/0233: the reforming step being a steam reforming step
- C01B 2203/1205: Composition of the feed
- C01B 2203/1235: Hydrocarbons
- C01B 2203/1264: Catalytic pre-treatment of the feed
- C10G 2300/1088: Olefins
- C10G 2300/202: Heteroatoms content, i.e. S, N, O, P
- C10G 2300/207: Acid gases, e.g. H2S, COS, SO2, HCN
- Y02P 20/52: using catalysts, e.g. selective catalysts
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C01B: NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; {METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C}
- C10K: PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS

## Abstract

The invention relates to a process and an apparatus for producing an olefin-containing feed stream for a steam reforming plant. According to the invention, the olefin-containing hydrocarbon starting material is for this purpose heated, vaporized and catalytically hydrogenated. The hydrogenation product stream obtained is separated in a separation apparatus into a gaseous reforming feed stream, which is fed to a steam reforming plant, and a gaseous recycle stream. Here, the entry temperature of the hydrogenation input stream into the hydrogenation reactor is regulated via the degree to which it is heated and/or via the size of the recycle stream. Safe operation of the hydrogenation reactor over a wide range of olefin contents in the hydrocarbon feed is made possible in this way.

## Claims

### Claim 1

A process for producing a feed stream for a steam reforming plant containing at least one reforming stage, the process comprising the following steps:
a) providing a first liquid input stream containing olefins and a second input stream comprising hydrogen;
b) combining of the first input stream and the second input stream to form a hydrogenation input stream;
c) heating of the hydrogenation input stream in a heating apparatus and vaporization of the hydrogenation input stream in a vaporization apparatus, thereby forming a heated and vaporized hydrogenation input stream;
d) introducing the heated and vaporized hydrogenation input stream into a hydrogenation reactor comprising at least one hydrogenation zone, at least partially converting the olefins present in the heated and vaporized hydrogenation input stream in the hydrogenation reactor under olefin hydrogenation conditions, and then discharging a gaseous olefin hydrogenation product stream from the hydrogenation reactor;
e) separating the gaseous olefin hydrogenation product stream in a separation apparatus into a gaseous reforming feed stream which is fed into a steam reforming plant and a gaseous recycle stream;
f) cooling of the gaseous recycle stream, with this being at least partially condensed and subsequently introduced into a phase separation apparatus in which it is separated into a gaseous partial recycle stream and a liquid partial recycle streams; and
g) discharging the gaseous partial recycle stream and the liquid partial recycle stream from the phase separation apparatus, with the gaseous partial recycle stream being combined with the second input stream and the liquid partial recycle stream being combined with the first input stream and/or being recirculated to process step (b),
wherein an entry temperature of the heated and vaporized hydrogenation input stream into the hydrogenation reactor is regulated by means of the heating apparatus (process step (c)) and/or by means of the separation apparatus (process step (e)).

### Claim 2 (depends on 1)

The process according to claim 1, wherein the heating apparatus in process step (c) is configured as a heat exchanger in which the hydrogenation input stream is heated by indirect heat exchange with a hot gas stream selected from the group consisting of a hot crude synthesis gas product stream from the steam reforming plant, a hot flue gas stream from the reformer furnace, a hot product gas stream from a CO conversion plant (CO shift) located downstream of the steam reforming plant, and combinations thereof, where the entry temperature of the heated and vaporized hydrogenation input stream into the hydrogenation reactor is regulated via the size of the hot gas stream which is conveyed through a bypass conduit around the heat exchanger.

### Claim 3 (depends on 1)

The process according to claim 1, wherein the entry temperature of the heated and vaporized hydrogenation input stream into the hydrogenation reactor is regulated by means of the separation apparatus via the size of the gaseous recycle stream.

### Claim 4 (depends on 1)

The process according to claim 1, wherein the total olefin content of the first input stream comprising olefins is in the range from 2 to 15 mol %.

### Claim 5 (depends on 1)

The process according to claim 1, wherein the total olefin content of the first input stream comprising olefins is in the range from 10 to 50 mol %.

### Claim 6 (depends on 1)

The process according to claim 1, wherein the entry temperature of the heated and vaporized hydrogenation input stream into the hydrogenation reactor is regulated both by means of the heating apparatus via the size of a bypass stream and also by means of the separation apparatus via the size of the gaseous recycle stream and in that the total olefin content of the first input stream comprising olefins is in the range from 2 to 50 mol %.

### Claim 7 (depends on 1)

The process according to claim 1, wherein the gaseous partial recycle stream is combined with the second input stream and compressed together or in that the gaseous partial recycle stream is combined with the second input stream after the second input stream has previously been compressed.

### Claim 8 (depends on 1)

The process according to claim 1, wherein an at least partial conversion of organic sulfur compounds present in the first input stream also occurs in the hydrogenation reactor under conditions of hydrodesulfurization (HDS) to give desulfurized hydrocarbons and hydrogen sulfide, with the hydrogen sulfide formed being separated off from the reforming feed stream before the reforming feed stream is fed to the steam reforming plant.

### Claim 9 (depends on 1)

The process according to claim 1, wherein the cooling in process step (f) is effected in a number of stages, with at least one cooling stage being configured as a heat exchanger in which cooling of the gaseous recycle stream occurs by indirect heat exchange with the first input stream introduced into the process or the hydrogenation input stream.

### Claim 10 (depends on 9)

The process according to claim 9, wherein at least one further cooling stage in which cooling of the gaseous recycle stream occurs by indirect heat exchange with a cooling medium, in particular cooling water, is present.

### Claim 11 (depends on 1)

The process according to claim 1, wherein the gaseous recycle stream is cooled to such an extent that at least half of it is condensed, so that at least 50 mol %; of the recycle stream is present in liquid form.

### Claim 12 (depends on 1)

The process according to claim 1, wherein the steam reforming plant comprises a prereforming stage in which higher hydrocarbons are at least partly converted into methane under prereforming conditions.